Abstract:
A process for distillation of two materials of differing boiling points particularly propane, ethane or carbon dioxide from natural gas is described in which the conventional distillation tower is divided into a first tower (102) at higher pressure than a conventional tower and a second tower (104) at lower pressure. Liquid drawn from the first is expanded to the lower pressure through two or more stages (111,112) with cool extracted (65,62) at each stage and used to cool (65,62) gas (51) withdrawn from the top of the first tower to keep the top tray at a required temperature. Gas (19) withdrawn from the second tower (104) is compressed and cooled for return to the first tower as a reflux. The use of the cool from the expanded liquid and the use of the two towers provides an improved thermo-dynamic efficiency and avoids the use of costly turbo-expanders.

Description:
This application is a continuaion-in-part of Ser. No. 06/727,765, filed 4-26-85 now abandoned. 
    
    
     CBACKGROUND OF THE INVENTION 
     This invention relates to a distillation process for the separation of close boiling point materials. Such a process is used in the extraction of various materials generally using a distillation tower and examples of such separations are: 
     (1) recovering ethane from nature gas; 
     (2) recovering propane from natural gas; 
     (3) recovering carbon dioxide from natural gas; 
     (4) recovering helium from natural gas; 
     (5) rejecting nitrogen from natural gas; 
     (6) separating ethane/ethylene; 
     (7) separating propane/propylene; 
     (8) separating normal butane/iso-butane; 
     (9) separating tritium/deuterium/light water; 
     (10) separating ethyl benzene/styrene; 
     (11) separating benzene/toluene/xylene. 
     The use of turbo-expanders has become popular in the last fifteen years for obtaining high recoveries of propane and ethane from natural gas. Early turbo-expander process designs resulted in ethane recoveries of 60% to 80% and propane recoveries of 90% to 98%. In 1978 and 1979 patents were filed by Morgan (Canadian Pat. No. 1,091,572) and Campbell et al (U.S. Pat. No. 4,157,904) which sub-cooled the high pressure low temperature flash liquid and then fed this liquid to the top of the demethanizer. These patents obtained 91% to 92.5% ethane recovery and 98% to 98.4% propane recovery. 
     Generally the natural gas is &#34;sweetened&#34; to remove sulphur compounds and carbon dioxide and then dehydrated using a molecular sieve adsorption system prior to feed to the turbo-expander plant. The supply gas is then cooled and chilled in the heat exchanger train which can include a gas/gas exchanger in which the residue gas is re-heated, a gas liquid exchanger which recovers &#34;cool&#34; from the demethanizer bottom product, a chiller using a propane refrigeration system and a demethanizer side re-boiler. 
     The chilled sweet gas is flashed in a high pressure low temperature flash vessel. Vapor from the vessel is expanded through a turbo-expander from which energy is taken to drive a compressor normally used to recompress the residue gas. Process gas leaving the turbo-expander enters a quench-fed demethanizer. Such processes normally achieve ethane recoveries between 60% and 80% and propane recoveries between 90% and 98%. 
     In the improvement of Campbell et al, liquid from the flash vessel at a temperature near its critical temperature is sub-cooled and introduced into the top of the demethanizer. The gas stream leaving the turbo-expander enters the demethanizer near the bottom. This process results in an improvement in ethane recoveries to approximately 92.5%. However, it operates at low thermodynamic efficiency and requires the use of turbo- expanders which have been found to be complex and expensive to maintain. 
     SUMMARY OF THE INVENTION 
     It is one object of the present invention, therefore, to provide an improved distillation process which obtains as good or better separation recoveries but with an improved thermodynamic efficiency and in many cases reduced equipment cost. 
     According to a first aspect of the invention, therefore, there is provided a method for separating a supply material into two materials of different boiling points comprising feeding supply material to vessel means arranged to form a mixed gas and liquid phase such that one material separates into said liquid phase in said vessel means and the other material separates into said gas phase, said liquid phase including no higher proportion of said other material than a required purity proportion and extracting said materials from said vessel means, characterized in the steps of providing said vessel means as two separate vessels, arranging said supply and said vessels such that the pressure in one of said vessels is higher than the other, transferring material from said liquid phase from said higher pressure vessel to the other vessel, said liquid phase having a proportion of said other material higher than said required purity proportion, and letting said liquid phase down in pressure as it is transferred so as to convert some of said liquid phase to said gas phase and causing cooling thereof. 
     According to a second aspect of the invention there is provided a method of separating a supply material into two materials at different boiling points comprising feeding supply material to vessel means arranged to form a mixed gas and liquid phase within said vessel means, exchanging said gas and liquid phases such that one material separates into said liquid phase in said vessel means and the other material separates into said gas phase, said liquid phase including no higher proportion of said other material than a required purity proportion, and extracting said materials from said vessel means, characterized in that liquid phase material to be separated is reduced in pressure to cause cooling thereof and cool is transferred therefrom to material at a top end of said vessel means to cool material prior to introduction into a top end of said vessel means to maintain said top end at a required temperature. 
     Improved efficiency can be obtained therefore by using a liquid in the process preferably that passing between a first portion of the distillation tower and the second low pressure portion of the distillation tower, letting that liquid down in pressure so as to obtain high cooling of the liquid and gas content and extracting that cool for cooling the top end of the distillation tower. The gas at low pressure can be re-compressed for returning to the high pressure portion of the distillation tower. 
     This technique can enable a significant reduction in power necessary for compression and for cooling and can in some circumstances avoid the use of turbo-expanders which, as explained before, have been found to have a high equipment cost. 
     The splitting of the distillation tower into a high pressure portion and a low pressure portion enables the high pressure portion to be operated at a much higher pressure than normal thus reducing the amount of recompression required for ethane and propane recovery from natural gas. In addition the warmer operating temperatures at the high pressure also reduce the possibility of carbon dioxide freezing on the trays which is often a problem in ethane recovery processes. The higher operating temperature also eases the requirement for the refrigerant for the over-head condenser. 
     The low pressure portion can operate at a much lower pressure than conventional towers thus obtaining a much better separation of the desired products and allowing a much lower re-boiler temperature so that often the re-boiler heat duty can be used to assist in refrigerating the feed. 
     The high pressure cold separator can be operated above the critical pressure so that the feed gas is now a single phase. This fluid can be expanded using a let down turbine for optimum refrigeration and recovery of energy. In conventional processes this fluid must first be expanded across a valve to a pressure less than the critical pressure where it can be flashed and the vapor is then expanded using a turbo-expander. The conventional process loses the energy that could have been recovered when flashing from the high pressure to that pressure below the critical pressure. 
     The re-cycled vapor from the low pressure tower can often be totally condensed to provide a very valuable reflux to assist the separation in the high pressure tower. 
     With the foregoing in view, and other advantages as will become apparent to those skilled in the art to which this invention relates as this specification proceeds, the invention is herein described by reference to the accompanying drawings forming a part hereof, which includes a description of the best mode known to the applicant and of the preferred typical embodiment of the principles of the present invention, in which: 
    
    
     DESCRIPTION OF THE DRAWINGS 
     FIG. 1 is a schematic layout according to the invention showing a system suitable for propane or ethane recovery. 
     FIG. 2 is a schematic layout according to the invention showing a system suitable for ethane recovery. 
     FIG. 3 is a schematic layout according to the invention showing an alternative system suitable for ethane recovery. FIG. 3 has more equipment than FIG. 2 but can achieve a higher recovery with less power demand and is more economical for large plants. 
     FIG. 4 is schematic layout according to the invention showing a system suitable for ethane or propane recovery from natural gas containing asphaltenes. 
     FIG. 5 is a schematic layout according to the invention showing a system suitable for recovering carbon dioxide from natural gas. Such carbon dioxide is often used for miscible flooding to achieve enhanced oil recovery. 
    
    
     DETAILED DESCRIPTION 
     The method shown in FIG. 1 is specifically designed for the separation of propane from natural gas. However, it will be appreciated that minor modification of the method can be made as described hereinafter and within the knowledge of a man skilled in the art for the separation of ethane or for other materials as stated above. 
     Natural gas enters the system on a feed line 1 and is introduced into an inlet plant separator 100 which removes heavy hydro-carbons in the condensed liquid phase. The liquid phase passes via a path to be described in detail hereinafter to a central area of a low pressure distillation tower 104. The gas phase from the vessel 100 passes via a path to be described hereinafter to a high pressure distillation tower 102. 
     The towers 102 and 104 operate together to form a distillation tower system so that recovered propane and higher boiling point materials are obtained on the line 68 from the bottom of the lower tower and residue gas is obtained on the line 59 from the top of the upper or high pressure tower 102. 
     The liquids from the vessel 100 are passed along a line 2 through a let down valve 114 to a flash vessel 101 from which the liquid phase which may include asphaltenes on the line 16 are passed to a central area through a let down valve 110 and line 17 to the lower tower 104. 
     Flash vapor from the vessel 100 leaves via stream 4 and is dehydrated in a molecular sieve dehydrator 108 of conventional form. Vapor from the dehydrator passes along a line 5 through a heat exchanger indicated at 86. 
     For convenience of illustration heat exchangers are shown as a single circle on the supply line with the corresponding portion of the heat exchanger shown on a separate part of the system and using the same reference numeral. Thus heat exchanger 86 has as its counterpart portion a heat exchanger on the line 59 immediately up stream of a compressor 73 and air cooler 83. Similar heat exchanger systems are shown in the drawing and will be described in more detail hereinafter. 
     For convenience of explanation and study, various temperature examples are shown on the drawings indicating the temperature of the stream at a particular point in the system while these temperature may not be referred to specifically in this description. 
     Stream 5 is cooled in the heat exchanger 86 and in a propane refrigerant exchanger 97. The propane refrigerant pressure on exchanger 97 is controlled to maintain the proper bottom product temperature for a stream 31 leaving the bottom of the high pressure tower 102 much in the same way that heat to a re-boiler is controlled to maintain a bottom product or bottom tray temperature in a conventional column. 
     Stream 8 leaving the exchanger 97 expands across a valve 113 to reduce the pressure from the supply pressure to the order of 750 PSIA. The expanded stream enters the high pressure tower 102 including a plurality of trays schematically indicated at 103. The trays are of a conventional form and act to repeatedly contact gases moving upwardly in tower with liquid moving downwardly in the tower to obtain the proper separation of the higher boiling point materials from the lower boiling point materials. The tower 102 in this example can have twelve theoretical trays which is approximately seventeen actual trays. 
     The bottom product in liquid phase in stream 31 passes to a heat exchanger 90 which acts as a sub-cooler and takes cool from the corresponding portion 90 shown on the line 59. The stream is then expanded through a valve 111 to a pressure of the order of 216 PSIA thus reducing the temperature significantly as shown. The stream then passes through a further heat exchanger 65 which has as its counter part heat exchanger 65 on a line 51 carrying gas from the top of the lower 102. 
     The material balance and process conditions at the inlet to and exit from the tower 102 together with the other points in the process are set out in detail in a table hereinafter. 
     The cooled product in the stream 31 is thus heated by the exchanger 65 and acts at the same time to significantly cool the gas in the stream 51 from the top of the tower 102, as shown by the indicated temperature values. This transfer of cool provides the improved thermodynamic efficiency since the cool obtained from the expanded liquid is directly used to cool the gas phase at the top of the tower 102 to obtain the necessary low temperature at the top of the tower 102 as will be described in more detail hereinafter. 
     The stream 31 is then introduced into an economizer/separator 103 in the form of a flash vessel. Liquid from the vessel 103 passes along a line 35 through a further let down valve 112 and a further heat exchanger 62 into the top of the lower tower 104. The counter part for the exchanger 62 is found again on line 51 so that again the expansion of the liquid as it passes from the upper tower 102 to the lower tower 104 provides a cooling effect which is directly transmitted to the gas at the top of the tower 102. 
     The pressure within the lower tower 104 is controlled to be of the order of 45 PSIA in this example. Generally, the pressure is arranged to be significantly less than the pressure of a convention distillation tower in a process of this type. 
     The lower tower 104 includes a number of trays 103 as previously described in relation to the tower 102. In addition the tower 104 includes a re-boiler 92 of conventional form at the bottom of the tower in order to control the bottom temperature. Liquid phase extracted at the bottom of the tower along the line 66 is transmitted by a pump 74 along the line 68. 
     Gas phase extracted from the top of the tower 104 along a line 19 has cool extracted by exchangers 96A and 94A which have their counterparts on a line 28 and indicated at 94 and 96 respectively. The gas on line 19 is then compressed in a compressor 71, cooled in an aerial cooler 81, further compressed in a compressor 72 and further cooled in a second aerial cooler 82. The product leading to the compressor 72 is supplemented by gas phase on line 30 from the economizer 103 which again has cool extracted by exchangers 96B, 94B. 
     From the air cooler 26 the product is passed through an amine contactor for removing carbon dioxide indicated at 106 and a dehydrator 107 prior to passing through the exchangers 94 and 96 and introduction into the top tower 102 at a position above the bottom and below the top. In between the exchangers 94 and 96, a propane refrigerant system similar to or common to the exchanger 97 is applied to the line indicated at 95 for further condensing the product into a mixed liquid and gas phase as it is applied to the tower 102. 
     The product re-introduced to the mid-section of the tower 102 acts as a reflux to assist in the separation in the tower 102. 
     The vapor stream leaving the tower 102 on line 51, as previously explained in cooled by the exchangers 62, 65 to condense the stream with liquid and gas phases being separated in a vessel 105. From the vessel 105 thegas phase is extracted on the line 59 and passed through the heat exchangers 90, 96, 86 together with the compressor 73 and aerial cooler 83. Liquid from the vesel 105 is pumped by a pump 69 onto the top tray of the tower 102. 
     It will be noted therefore that the top tower 102 can be operated at a significantly higher pressure than would be used in a conventional than is of the order of tower in a similar process. The pressure of the conventional process and of the present invention can readily be determined by one skilled in the art by simple experimentation. The temperature gradient is controlled by the temperature of the reflux material from the pump 69. A re-boiler can be applied at the bottom if required but in the present example the bottom temperature is controlled by the refrigerant exchanger 97 which controls the temperature of the material introduced into the bottom of the tower 102. The tower in this example also acts as a flash vessel with the mixed phase being introduced at the bottom and the gas passing from that phase through the trays in exchanging relation therewith to provide the proper separation over the proper temperature gradient. 
     The expansion of the liquid phase from the top tower 102 obtains sufficient cool to condense the gas phase at the top of the top tower to provide the reflux through the pump 62. Thus the top tray of the tower 102 can be controlled at the required temperature. 
     The let down or expansion valves 111 and 112 are of the Joule-Thompson type which are simple devices having little or no moving parts and thus are inexpensive to obtain and simple to maintain. 
     The table of material balance and process conditions for one example is as follows: 
     
         __________________________________________________________________________  Stream Number       31    19     28   59   66  8    Internal             Deethanizer                    Recycle                         Residue                              Liquid  Feed Refrigerant             Vapor  Vapor                         Gas  Product__________________________________________________________________________Temperature  -34.6       -43.8 -69.9  -61.7                         120.0                              44.8(F.)Pressure  809  752   45     751  1200 46(PSIA)Flowrate  1585.54       525.68             206.50 456.56                         1515.00                              114.66(lb mols/h)Composition:N2     .0079       .0015 .0002  .0019                         .0083                              .0000CO2    .0221       .0317 .0456  .0000                         .0121                              .0000Methane  .8395       .5024 .2786  .6120                         .8880                              .0000Ethane .0826       .2862 .6030  .3449                         .0909                              .0002Propane  .0316       .1263 .0686  .0382                         .0008                              .4858Butane+  .0463       .0519 .0040  .0030                         0    .5140__________________________________________________________________________ 
    
     In an alternative arrangement (not shown) the simple valve 113 could be replaced by a flash vessel followed by a let down turbine with the power from the turbine being used to drive a central gas compressor immediately prior to the compressor 73. Such an arrangement ca be used where the supply pressure is considerably in excess of the acceptable pressure of the top tower 102. The top tower 102 cannot have or operate at a pressure higher than the critical pressure for the material concerned. 
     In a modification used for ethane recovery, the let-down valves 111 and 112 can each be replaced by a plurality of such valves, each followed by an exchanger communicating cool to the line 541. This can be used to avoid the temperature reaching a low level at which the carbon dioxide freezes. 
     In a further alternative arrangement the material passing through the exchanger 86 on the line 5 can be divided into a second line which carries exchangers cooperating respectively with the re-boiler 92 and with a further chiller on the outlet line 68 from the bottom of the lower tower 104. 
     Turning now to FIGS. 2 and 3, the conventional turbo-expander process is compared with two methods of this invention as shown in FIGS. 2 and 3. 
     For convenience of illustration, the heat exchangers in FIGS. 2, 3, 4 and 5 are shown as a single circle on the supply line with the corresponding portion of the heat exchanger shown on a separate part of the system and using the same reference numeral. In some situations, such as Exchanger 72 on FIG. 2, one stream is cooled by two other streams in parallel. This is shown by the equation on FIG. 2: H72=H76+H86. The negative sign with the exchanger number indicates that the stream is being cooled; no sign indicates that the stream is being heated. In the case of compressors, no sign indicates compression, a negative sign indicates a turbo-expander as shown on FIG. 1. Compressor and turbo-expander powers consider an 80% adiabatic efficiency. Pump powers assume a 50% adiabatic efficiency. 
     The Material Balances for FIGS. 2, 3, 4, and 5 (Tables 10, 16, 23, and 30 respectively) each have a Stream 9, which indicates the error in the computer simulation between the Feed and the sum of the Product Streams. This error is due to the recycle nature of the process. The error can be reduced by continuing the calculation through further iterations or by making &#34;educated&#34; adjustments to the compositions of the recycle streams and repeating the computer simulation. 
     Tables 3 to 7 and FIG. 1 describe the conditions used for determining Case 1, The Conventional Turbo-Expander Process. 
     1. Two Tower Process (FIG. 2) 
     FIG. 2 is a simple form of this invention and should have a cost roughly comparable to the conventional process on plants having a capacity greater than 2,000,000 m3API/d. On smaller plants, where the cost of the turbo-expander is disproportionate, the invention will cost less since no turbo-expander is required. It is thus now possible to economically obtain high recoveries in small plants. Turbo-expanders and liquid expansion turbines can be used in the processes of this patent and are probably economical in capacities over 3,000,000 m3API/d. 
     Table 8 shows the temperature, pressure, and other stream properties for the process shown on FIG. 2 and the design basis shown on Table 2. Table 9 shows the duties for the heat exchangers and the power required for the pumps and compressors shown on FIG. 2. Table 10 shows the process material balance. Table 11 shows the major stream compositions. Table 12 shows the column temperature, pressure, and other property profiles for the gas fractionator shown on FIG. 2. Table 13 shows the column temperature, pressure, and other property profiles for the demethanizer shown on FIG. 2. 
     Examining the tables listed above and FIG. 2, it is seen that the dehydrated sweet gas inlet, Stream 4, is split into Stream 17 and Stream 20. Stream 17 is cooled in Exchanger 85 which derives its cool from the C2+ Product, Stream 38. Stream 20 is cooled in Exchanger 70 with Residue Gas, Stream 63, then chilled with Chiller 71 which derives its cool from a refrigeration system. The above two streams are then recombined in Stream 24 which is cooled in Exchanger 72 which derives its cool from two sources, Exchanger 76 which derives its cool from the Cold Recycle Gas, Stream 40, and Exchanger 86 which derives its cool from the Residue Gas, Stream 62. Finally, the gas is partially condensed in the Demethanizer Reboiler, Exchanger 79. The fluid is then flashed from 6120 kPa a to 3585 kPa a resulting in the fluid being approximately 35% liquid at the inlet to the Gas Fractionator. 
     There is no need for a reboiler on the Gas Fractionator because it is stripped with recycle vapor. The temperature of the recycle vapor is controlled by controlling the refrigerant pressure in the Recycle Chiller, Exchanger 78. Thus if there is too much vapor in Stream 40 for the Recycle Compressor 93, the temperature of recycle vapour, Stream 48 is raised by reducing the refrigeration transferred in the Recycle Chiller, Exchanger 78. 
     The liquid leaving the Gas Fractionator, Stream 30, is subcooled using the Gas Fractionator Overhead, Stream 60, in Exchanger 73. This liquid is then flashed into the shell side of the Gas Fractionator Condenser, Exchanger 74. The flashing liquid provides cool to the condenser then the flashing liquid enters the Demethanizer. The C2+ product specification is controlled by the Demethanizer Reboiler, Exchanger 79, in the conventional manner. 
     The recycle vapour leaving the Demethanizer, Stream 40, is heated in two exchangers 76 and 77 then compressed in a two stage compressor. The recycle vapour is then cooled in the Compressor Aftercooler, Exchanger 84 and the Recycle Warm Gas/Gas Exchanger 77, then chilled in the Recycle Chiller, Exchanger 78. 
     Exchanger 75 has its duty set at 0 because it is not required for the present configuration for ethane recovery. However, it is used in the propane recovery configuration to partially condense the Recycle Gas Stream 48. Other changes are made for propane recovery; the partially condensed recycle stream enters the middle of the Gas Fractionator and the Raw Gas Feed, Stream 27, enters the bottom of the Gas Fractionator. The process control for the gas fractionator is then achieved by varying the refrigerant pressure on the Feed Chiller, Exchanger 71, rather than the Recycle Chiller, Exchanger 78. In the propane recovery situation, the Deethanizer Reboiler, Exchanger 79, is located on Stream 18 following Exchanger 85 rather than on Stream 25 following the Cold Gas/Gas Exchanger 72. Propane recoveries of 98 to 99% can be achieved for this configuration for comparable capital costs and energy requirement as for the conventional process shown on FIG. 1. 
     2. FIG. 3 THREE TOWER PROCESS 
     Tables 14 to 20 describe the Three Tower Process of this invention shown on FIG. 3 in a similar fashion to the description of FIG. 2. In the Three Tower Process the separation is improved with a reduction in energy requirement as shown in Table 1. This process will be preferred to that of FIG. 2 for larger plants where the saving in power requirement and the increased recovery make its larger capital expenditure more economical. Note that for very large plants the reduced expense for compression may result in less capital cost for FIG. 3 type designs&#39; than FIG. 2 type designs&#39;. For very large plants a 4 tower process with an economizer tower between each stage may be desirable. 
     A variation of this process, can add a separator to Stream 48, and remove a portion of the liquid taken from this separator as ethane product. Stream 37 then becomes C3+ Product and the former demethanizer is operated as a deethananizer. The temperature of the Deethanizer Reboiler, Exchanger 79, now is too high to cool Stream 25 and must be located on Stream 18. The advantage of this variation is that ethane product can be produced with fewer pieces of equipment and probably less energy requirement. The disadvantage is that ethane recovery is reduced and some sacrifice in the quality of the ethane product may result. 
     The chilling train for the raw gas and the cool recovery from the residue gas for the FIG. 3 process is similar to FIG. 2. The Gas Fractionator liquid product is subcooled in Exchanger 73 in similar fashion. The subcooled liquid is flashed into the Economizer Tower which provides a few stages of distillation and also acts in a similar fashion to an economizer in a conventional refrigeration system. This tower heightens the concept of achieving separation while obtaining refrigeration. 
     Since the vapor leaving the Economizer, Stream 50, is leaner than the feed, Stream 4, it is preferable to give it priority for low temperature chilling and inject it into a higher tray in the Gas Fractionator. Following the Lean Recycle Gas on FIG. 3, Stream 53 leaves the Compressor 94, is cooled in the Lean Gas Aerial Cooler 84, then cooled in the Lean Warm Gas/Gas Exchanger 97. The Lean Recycle Gas, Stream 55, is then chilled in Exchanger 87 using a conventional refrigeration system. The Chilled Lean Recycle Gas, Stream 56 is then partially condensed using Residue Gas in Exchanger 75 and then further condensed in Exchanger 98 using Rich Recycle Gas (Exchanger 76) and Lean Recycle Gas (Exchanger 96). 
     The Rich Recycle Gas, Stream 40, is compressed, cooled, and temperature controlled in the same manner as the Recycle Stream in FIG. 2. Also, the Feed Chiller, Exchanger 71, is temperature controlled to maintain the proper amount of lean recycle gas. 
     3. FIG. 4 PROCESSING NATURAL GAS WITH ASPHALTENES 
     Asphaltenes are heavy naphthenic molecules that must be removed before the molecular sieve dehydrator. A dry gas filter is traditionally placed in front of the dehydrator for this purpose. Some natural gas streams contain too many asphaltenes for them to be practically removed by a filter alone. The process shown on FIG. 4 recovers practically all of the asphaltenes with the Low Temperature Separator and Stabilizer prior to the Dry Gas Filter and Molecular Sieve Dehydrator. Another advantage of this system, is that the bulk of the C5+ Product is recovered by the Stabilizer as stabilized condensate; thus LPG Product is produced by the deethanizer in Stream 37. Other advantages of this system are that the Deethanizer Reboiler, Exchanger 79, operates at a lower temperature and that the Gas Fractionator Condenser, Exchanger 74, requires less methane recycle to obtain the desired amount of chilling. 
     Following FIG. 4, Plant Inlet Gas, Stream 19, enters the Inlet Separator at 1140 kPa a. Liquid from this separator, Stream 20, is pumped into the Low Temperature Separator. Vapour from the Inlet Separator joins the Stabilizer Overhead, Stream 35, and the compressed Deethanizer Overhead, Stream 23, and is compressed in Compressor 91 to 3985 kPa a. Stream 25 is cooled with the Aftercooler 81, and then with the cooling train. As in other cryogenic processes, the raw gas stream is split into two streams, Streams 27 and Stream 14. Stream 27 is cooled with the Warm Gas/Gas Exchanger 71 which recovers its cool from the Cool Deethanizer Overhead, Stream 55, in Exchanger 78, and from the Cool Residue Gas, Stream 63, in Exchanger 88. 
     The other raw gas stream, Stream 14, is cooled with LPG Product Stream 58, in Exchanger 85; further cooled with Low Temperature Liquid, Stream 31, in Exchanger 72; and finally cooled with the Deethanizer Reboiler, Exchanger 89. The two raw gas streams then recombine and enter the Low Temperature Separator at -8.7° C. 
     If the inlet stream has not been suitably dehydrated, then the conventional process is to spray a solution containing 80% ethylene glycol/water on to the inlet tube sheets of the heat Exchangers mentioned above to prevent hydrate formation. The ethylene glycol/water solution is removed from the Low Temperature Separator and regenerated in the conventional manner. 
     The Material Balance, Table 23, shows that 99% of the C6+ (n-octane and heavier components) are removed in the Low Temperature Separator and recovered in the stablized condensate in the Stabilizer. Asphaltenes are very much less volatile than n-octane, so essentially all of them are recovered prior to the Dry Gas Filter which is part of the Dehydration Package following Stream 40. 
     The remainder of the process follows the same principles as described in FIG. 2. Stream 41, leaving the Dehydration Package, is chilled in Exchanger 73 using a conventional refrigeration system. It is partially condensed in Exchanger 74 which derives its cool from Cold Residue Gas, Stream 62, in Exchanger 87, and from Cold Lean Recycle Gas, Stream 54, in Exchanger 77. It is then flashed into the Gas Fractionator. 
     Liquid from the Gas Fractionator, Stream 50, is subcooled in Exchanger 75 using the Gas Fractionator Overhead, Stream 61. The liquid is then flashed into the Gas Fractionator Condenser, Exchanger 76 before entering the Deethanizer. 
     LPG and Condensate Product specifications are met in the conventional manner by controlling the tower bottom temperatures with their reboilers, Exchangers 89 and 79 respectively. Exchanger 89 has a temperature controlled bypass between Streams 16 and 17. Exchanger 79 is supplied with a temperature-controlled flow of heating medium. 
     The Deethanizer Overhead is heated in Exchangers 77 and 78 as previously discussed, then compressed in Compressor 90 with Aftercooler 80. 
     4. Carbon Dioxide Solid Formation 
     The ethane recovery processes discussed above were much more resistant to CO2 solid formation than the conventional processes because of their higher operating temperatures and the fact that solids would form at the outlet of expansion valves rather on the distillation trays. These expansion valves can be located very near the heat exchanger or vessel following them. In this manner the freezing gas is immediately warmed or diluted so that the freezing problem is reduced. The freezing problem can be further reduced by using two or more expansion valves with heat exchangers between them rather than one valve. In this manner, natural gas streams with high CO2 contents can be processed for ethane recovery without solid formation problems. Traditionally, CO2 contents above 2% were virtually impossible to treat and the content was preferable less than 1%. The new technology is so adept at handling CO2 that this technology can be used to recover CO2 from natural gas. 
     5. Carbon Dioxide Recovery from Natural Gas (FIG. 5) 
     FIG. 5 shows one configuration for recovering carbon dioxide from moderately high pressure (2800 kPa a) natural gas. As with propane and ethane recovery, there will be many variations of the process depending upon feed composition and pressure, product values and economics. In fact, this process is much more sensitive to feed composition than the previous processes because the process design must prevent CO2 solid formation. 
     This process uses the same technology as described in FIGS. 2, 3, and 4. Tables 28 to 35 describe an example of this technology shown on FIG. 5. Following the Inlet Gas, Stream 1, on FIG. 5, is cooled in the Warm Gas Exchanger 70 which derives its cool from the Warm Residue Gas, Stream 42, in Exchanger 85 and the CO2 Product, Stream 61, in Exchanger 76. The feed is then chilled in Exchanger 71 using a conventional refrigeration system. The feed is further cooled using cool from the Reboiler, Exchanger 72, and cool from flashing liquid streams between the towers, Exchangers 73 and 74. 
     Stream 20, the overhead from the low pressure column, Tower #3, is heat exchanged and compressed with two stages of compression and finally chilled in Exchanger 77 using a conventional refrigeration system. The rich cycle gas is compressed to 6890 kPa a, then flashed to the operating pressure of Tower #2, 2645 kPa a. This results in Stream 30, the rich recycle inlet to Tower #2, having a temperature of -59.5 C. which is very close to its freezing point, -60.6 C. (Table 32). In order to minimize the chance of freezing, the expansion valve between Stream 29 and Stream 30 should be located near Tower #2. The risk for freezing Stream 30 can also be reduced by installing an expansion valve between Stream 59 and Tower #1 and reducing the pressure differential between Streams 29 and 30. Stream 30 will be warmer then and should be injected to a lower tray in Tower #2. 
     Processing of the Lean Recycle Gas leaving Tower #2 is similar to the other processes above. In order to obtain reflux for Tower #1 while avoiding a reflux problem, it is necessary to compress the Tower #1 overhead as shown. The quality of the residue gas (the amount of CO2 that it contains) is adjusted by adjusting Compressor 93 discharge pressure. Similarly, the amount of Tower #3 overhead vapor is adjusted by adjusting the Compressor 91 discharge pressure. If there were a pressure control valve between Stream 59 and Tower #2, the amount of Tower #2 overhead could be controlled by adjusting the backpressure on that control valve. In the present system, the amount of Tower #2 overhead can be controlled by controlling the amount of refrigeration supplied to Chiller 78. One means of optimizing the operation and obtaining maximum recovery is to control the pressures and refrigeration demands as mentioned above so that the volumes of recycle gas are at plant design and controlling the overhead reflux to produce a specification overhead product. Optimizing the process for a &#34;turn-down situation&#34; (where the plant is processing less than the design volume of inlet gas) will require a consideration of both the process and mechanical design. Similarily, optimizing the operation when treating a feed of different composition to the design composition requires a combined knowledge of the process and the mechanical equipment. 
     
                                           TABLE 3__________________________________________________________________________Conventional Turbo-Expander Process (FIG. 1)Stream Properties__________________________________________________________________________Stream      4           22           24           25__________________________________________________________________________Name        FEED        FEED         FEED         FEEDVapour frac.       1.0000      0.9939       0.9669       0.9665Temperature C.       21.0753     -14.4720     -34.2488     -34.4444   *Pressure Kpa a       6294.9131   6260.4395    6225.9658    6191.4922Molar Flow Kgmole/hr       297.7482    297.7482     297.7482     297.7482Mass Flow Kg/hr       5540.7427   5540.7427    5540.7427    5540.7427Volume Flow M3/hr       16.7591     16.7591      16.7591      16.7591Enthalpy KJ/hr       2.59635E+06 2.03601E+06  1.64025E+06  1.64023E+06__________________________________________________________________________Stream      26          30           31           32__________________________________________________________________________Name        FEED        LOW TEMP LIQ LOW TEMP LIQ LOW TEMP LIQVapour frac.       0.8033      0.0000       0.5186       0.8916Temperature C.       -57.5729    -57.5729     -99.5431     -33.0278   *Pressure Kpa a       6157.0186   6157.0186    1413.4252  * 1378.9514Molar Flow Kgmole/hr       297.7482    58.5608      58.5608      58.5608Mass Flow Kg/hr       5540.7427   1347.5385    1347.5385    1347.5385Volume Flow M3/hr       16.7591     3.6474       3.6474       3.6474Enthalpy KJ/hr       949612.3125 -37556.4492  -37556.4492  358203.8438__________________________________________________________________________Stream      37          60           61           62__________________________________________________________________________Name        C2+ PRODUCT LOW TEMP VAP EXPANDER OUT RESIDUE GASVapour frac.       0.0000      1.0000       0.8129       1.0000Temperature C.       -3.0858   * -57.5729     -109.2679    -106.2850  *Pressure Kpa a       1399.6356 * 6157.0186    1378.9514  * 1378.9514  *Molar Flow Kgmole/hr       24.1077   * 239.1874     239.1874     273.6406   *Mass Flow Kg/hr       966.0270    4193.2041    4193.2041    4574.7158Volume Flow M3/hr       2.1285      13.1117      13.1117      14.6307Enthalpy KJ/hr       -73117.6094 987170.0625  736226.0625  1.32713E+06__________________________________________________________________________Stream      63          64           65           66__________________________________________________________________________Name        RESIDUE GAS RESIDUE GAS  RESIDUE GAS  RESIDUE GASVapour frac.       1.0000      1.0000       1.0000       1.0000Temperature C.       -40.0000  * 15.5556    * 42.0263      196.1051Pressure Kpa a       1344.4777   1310.0039    1775.3999  * 8397.8135Molar Flow Kgmole/hr       273.6406    273.6406     273.6406     273.6406Mass Flow Kg/hr       4574.7158   4574.7158    4574.7158    4574.7158Volume Flow M3/hr       14.6307     14.6307      14.6307      14.6307Enthalpy KJ/hr       2.01775E+06 2.57809E+ 06 2.82837E+06  4.44477E+06__________________________________________________________________________Stream      68__________________________________________________________________________Name        RESIDUE GASVapour frac.       1.0000Temperature C.       48.8889   *Pressure Kpa a       8363.3398 *Molar Flow Kgmole/hr       273.6406Mass Flow Kg/hr       4574.7158Volume Flow M3/hr       14.6307Enthalpy KJ/hr       2.62310E+06__________________________________________________________________________ 
    
     
                                           TABLE 4__________________________________________________________________________Conventional Turbo-Expander Process (FIG. 1)Exchanger Duties and Compressor Power__________________________________________________________________________Stream  70          71        72     73__________________________________________________________________________Name    WARM GAS/GAS               GAS/LIQ HEX                         CHILLER                                COLD GAS/GASEnthalpy KJ/hr   560338.0625 395760.2813                         21.5396                                690620.9375__________________________________________________________________________Stream  79          82        90     91__________________________________________________________________________Name    REBOILER    AFTERCOOLER                         EXPANDER                                RECOMPRESSOREnthalpy KJ/hr   159602.0313             * 1.82166E+06                         250943.9844                                1.61640E+06__________________________________________________________________________Stream  92__________________________________________________________________________Name    BOOSTER COMPEnthalpy KJ/hr   250275.2500__________________________________________________________________________ 
    
     
                                           TABLE 5__________________________________________________________________________CONVENTIONAL Turbo-Expander Process (FIG. 1)Material BalanceStream       4      37         62         30__________________________________________________________________________Name         FEED   C2+ PRODUCT                          RESIDUE GAS                                     LOW TEMP LIQVapour frac. 1.0000 0.0000     1.0000     0.0000Temperature C.        21.0753               -3.0858  * -106.2850                                   * -57.5729Pressure Kpa a        6294.9131               1399.6356                        * 1378.9514                                   * 6157.0186Molar Flow Kgmole/hr        297.7482               24.1077  * 273.6406 * 58.5608Mass Flow Kg/hr        5540.7427               966.0270   4574.7158  1347.5385Volume Flow M3/hr        16.7591               2.1285     14.6307    3.6474Enthalpy KJ/hr        2.59635E+06               -73117.6094                          1.32713E+06                                     -37556.4492Density Kg/m3        57.4469               511.7144   20.3557    357.1277Mole Wt.     18.6088               40.0714    16.7180    23.0109Spec. Heat KJ/Kgmole-C        48.9815               106.6243   41.0687    87.3373Therm Cond Watt/m-K        0.0406 --         0.0223     0.0883Viscosity Cp 0.0130 --         0.0071     0.0447Sur Tension Dyne/cm        --     --         --         2.0911Std Density Kg/m3        --     --         --         --Z Factor     0.8335 --         0.8163     0.2213N2 Kgmole/hr 5.0123 0.0000   * 5.0123   * 0.4208CO2 Kgmole/hr        3.4056 0.4785   * 2.9272   * 0.9749Methane Kgmole/hr        262.8470               0.1276   * 262.7194 * 43.2417Ethane Kgmole/hr        15.6641               12.7527  * 2.9113   * 6.3379Propane Kgmole/hr        6.8591 6.7906   * 0.0685   * 4.2901i-Butane Kgmole/hr        1.0422 1.0410   * 0.0012   * 0.7885n-Butane Kgmole/hr        1.4193 1.4187   * 0.0006   * 1.1371i-Pentan Kgmole/hr        0.5360 0.5360   * 0.0000   * 0.4721n-Pentan Kgmole/hr        0.4764 0.4764   * 0.0000   * 0.4303n-Hexane Kgmole/hr        0.3374 0.3374   * 0.0000   * 0.3219n-Heptan Kgmole/hr        0.1488 0.1488   * 0.0000   * 0.1456Total Kgmole/hr        297.7482               24.1077  * 273.6406 * 58.5608__________________________________________________________________________ 
    
     
                                           TABLE 6__________________________________________________________________________Conventional Turbo-Expander Process (FIG. 1)Stream CompositionsStream       4      37         62         30__________________________________________________________________________Name         FEED   C2+ PRODUCT                          RESIDUE GAS                                     LOW TEMP LIQVapour frac. 1.0000 0.0000     1.0000     0.0000Temperature C.        21.0753               -3.0858  * -106.2850                                   * -57.5729Pressure Kpa a        6294.9131               1399.6356                        * 1378.9514                                   * 6157.0186Molar Flow Kgmole/hr        297.7482               24.1077  * 273.6406 * 58.5608Mass Flow Kg/hr        5540.7427               966.0270   4574.7158  1347.5385Volume Flow M3/hr        16.7591               2.1285     14.6307    3.6474Enthalpy KJ/hr        2.59635E+06               -73117.6094                          1.32713E+06                                     -37556.4492Density Kg/m3        57.4469               511.7144   20.3557    357.1277Mole Wt.     18.6088               40.0714    16.7180    23.0109Spec. Heat KJ/Kgmole-C        48.9815               106.6243   41.0687    87.3373Therm Cond Watt/m-K        0.0406 --         0.0223     0.0883Viscosity Cp 0.0130 --         0.0071     0.0447Sur Tension Dyne/cm        --     --         --         2.0911Std Density Kg/m3        --     --         --         --Z Factor     0.8335 --         0.8163     0.2213N2           0.0168 0.0000   * 0.0183   * 0.0072CO2          0.0114 0.0198   * 0.0107   * 0.0166Methane      0.8828 0.0053   * 0.9601   * 0.7384Ethane       0.0526 0.5290   * 0.0106   * 0.1082Propane      0.0230 0.2817   * 0.0003   * 0.0733i-Butane     0.0035 0.0432   * 0.0000   * 0.0135n-Butane     0.0048 0.0588   * 0.0000   * 0.0194i-Pentan     0.0018 0.0222   * 0.0000   * 0.0081n-Pentan     0.0016 0.0198   * 0.0000   * 0.0073n-Hexane     0.0011 0.0140   * 0.0000   * 0.0055n-Heptan     0.0005 0.0062   * 0.0000   * 0.0025__________________________________________________________________________ 
    
     
                                           TABLE 7__________________________________________________________________________Conventional Turbo-Expander Process (FIG. 1)Demethanizer Property ProfilesHyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN70  Date 1980/1/1   Time 8:54:8TRANSPORT PROPERTIESVAPOUR                LIQUID       THERMAL          THERMAL   SURFACESTAGEVISCOSITY       CONDUCTIVITY                 VISCOSITY                        CONDUCTIVITY                                  TENSIONNO.  CP     WATT/M-K  CP     WATT/M-K  DYNE/CM__________________________________________________________________________1    0.00711       0.02230   0.10148                        0.14760   10.09432    0.00756       0.02282   0.13269                        0.15648   12.65673    0.00809       0.02289   0.13963                        0.15282   12.98314    0.00833       0.02280   0.13495                        0.14725   12.43255    0.00839       0.02290   0.12897                        0.14234   11.81396    0.00841       0.02312   0.12389                        0.13822   11.28137    0.00844       0.02339   0.12262                        0.13552   11.05428    0.00868       0.02428   0.15435                        0.13756   12.78629    0.00869       0.02428   0.15287                        0.13685   12.674010   0.00876       0.02416   0.14981                        0.13521   12.431811   0.00892       0.02378   0.14288                        0.13148   11.859512   0.00915       0.02289   0.13108                        0.12504   10.808213   0.00928       0.02173   0.11781                        0.11777    9.549014   0.00926       0.02109   0.10871                        0.11205    8.565915   0.00930       0.02140   0.10847                        0.10783    8.2282__________________________________________________________________________ 
    
     
                                           TABLE 8__________________________________________________________________________Two Tower Process (FIG. 2)Stream Properties__________________________________________________________________________Stream      4            9            17           18__________________________________________________________________________Name        PLANT INLET  ERROR        GAS/LIQ IN   GAS/LIQ OUTVapour frac.       1.0000       --           1.0000       0.9193Temperature C.       21.0753      --           21.0753      -47.1435Pressure Kpa a       6294.9131    --           6294.9131    6191.4917Molar Flow Kgmole/hr       297.7482     0.0103       45.3592   *  45.3592Mass Flow Kg/hr       5540.7427    0.1116       844.0818     844.0818Volume Flow M3/hr       16.7591      0.0005       2.5531       2.5531Enthalpy KJ/hr       2.59635E+06  --           395530.7813  200441.0156__________________________________________________________________________Stream      20           21           23           24__________________________________________________________________________Name        GAS/GAS IN   GAS/GAS OUT  CHILLER OUT  COLD GAS INVapour frac.       1.0000       0.9857       0.9755       0.9696Temperature C.       21.0753      -23.1573     -30.0856     -33.0309Pressure Kpa a       6294.9131    6225.9653    6191.4917    6191.4917Molar Flow Kgmole/hr       252.3890     252.3890     252.3890     297.7482Mass Flow Kg/hr       4696.6606    4696.6606    4696.6606    5540.7427Volume Flow M3/hr       14.2060      14.2060      14.2060      16.7591Enthalpy KJ/hr       2.20082E+06  1.58932E+06  1.47173E+06  1.67218E+06__________________________________________________________________________Stream      25           26           27           30__________________________________________________________________________Name        REBOILER IN  REBOILER OUT GAS FRAC IN  GAS FRAC LIQVapour frac.       0.7304       0.6003       0.6485       0.0000    *Temperature C.       -60.0476     -62.5948  *  -81.1537     -76.4986  *Pressure Kpa a       6157.0181    6122.5444    3585.2734 *  3585.2734 *Molar Flow Kgmole/hr       297.7482     297.7482     297.7482     106.0311  *Mass Flow Kg/hr       5540.7427    5540.7427    5540.7427    2443.3013Volume Flow M3/hr       16.7591      16.7591      16.7591      6.6430Enthalpy KJ/hr       823984.6875  676019.7500  676019.7500  -240615.5625__________________________________________________________________________Stream      31           32           33           37__________________________________________________________________________Name        SUBCOOLD LIQ CONDENSER IN DC2 FEED     C2+ PRODUCTVapour frac.       0.0000       0.4010       0.6928       0.0000Temperature C.       -87.1484     -132.1353    -115.2480    -65.3441  *Pressure Kpa a       3516.3259    379.2116     275.7903  *  282.6850  *Molar Flow Kgmole/hr       106.0311     106.0311     106.0311     27.2160   *Mass Flow Kg/hr       2443.3013    2443.3013    2443.3013    1081.5333Volume Flow M3/hr       6.6430       6.6430       6.6430       2.3429Enthalpy KJ/hr       -325302.3125 -325302.3125 20515.0625   -234289.8750__________________________________________________________________________Stream      38           39           40           41__________________________________________________________________________Name        C2+ PRODUCT  C2+ PRODUCT  DC1 OVERHEADVapour frac.       0.0000       0.0000       1.0000       1.0000Temperature C.       -60.5575     15.5556   *  -115.1000 *  -40.0000  *Pressure Kpa a       6205.2813 *  6170.8076    275.7903  *  262.0008Molar Flow Kgmole/hr       27.2160      27.2160      78.8150   *  78.8150Mass Flow Kg/hr       1081.5333    1081.5333    1361.7679    1361.7679Volume Flow M3/hr       2.3429       2.3429       4.3000       4.3000Enthalpy KJ/hr       -217786.1563 -22696.3770  402775.1563  606865.2500__________________________________________________________________________Stream      42           43           44           45__________________________________________________________________________Name        1ST SUCTION  1ST DISCHARG 2ND SUCTION  2ND DISCHARGVapour frac.       1.0000       1.0000       1.0000       1.0000Temperature C.       32.2222   *  160.4082     51.6667   *  180.6932Pressure Kpa a       248.2112     985.9502     965.2659  *  3668.0107Molar Flow Kgmole/hr       78.8150      78.8150      78.8150      78.8150Mass Flow Kg/hr       1361.7679    1361.7679    1361.7679    1361.7679Volume Flow M3/hr       4.3000       4.3000       4.3000       4.3000Enthalpy KJ/hr       811394.3125  1.21108E+06  859362.3125  1.26341E+06__________________________________________________________________________Stream      46           47           48           60__________________________________________________________________________Name        WARM RECYCLE COOL RECYCLE CHILLED REC  GASFRAC OVHDVapour frac.       1.0000       1.0000       1.0000       1.0000    *Temperature C.       43.3333   *  -19.6698     -34.4444  *  -89.9262  *Pressure Kpa a       3640.4316    3612.8525    3585.2734 *  3543.9050 *Molar Flow Kgmole/hr       78.8150      78.8150      78.8150      270.5219  *Mass Flow Kg/hr       1361.7679    1361.7679    1361.7679    4459.0972Volume Flow M3/hr       4.3000       4.3000       4.3000       14.4157Enthalpy KJ/hr       796920.1250  592391.0625  542950.9375  1.09745E+06__________________________________________________________________________Stream      61           62           63           64__________________________________________________________________________Name        RESIDUE GAS  RESIDUE GAS  RESIDUE GAS  RESIDUE GASVapour frac.       1.0000       1.0000       1.0000       1.0000Temperature C.       -86.6202     -86.9536     -40.0000  *  15.5556   *Pressure Kpa a       3516.3259    3488.7468    3454.2729    3419.7991Molar Flow Kgmole/hr       270.5219     270.5219     270.5219     270.5219Mass Flow Kg/hr       4459.0972    4459.0972    4459.0972    4459.0972Volume Flow M3/hr       14.4157      14.4157      14.4157      14.4157Enthalpy KJ/hr       1.18214E+06  1.18214E+06  1.82624E+06  2.43775E+06__________________________________________________________________________Stream      66           68__________________________________________________________________________Name        SALES GASVapour frac.       1.0000       1.0000Temperature C.       102.8382     48.8889   *Pressure Kpa a       8397.8135    8363.3398 *Molar Flow Kgmole/hr       270.5219     270.5219Mass Flow Kg/hr       4459.0972    4459.0972Volume Flow M3/hr       14.4157      14.4157Enthalpy KJ/hr       3.24086E+06  2.59570E+06__________________________________________________________________________ 
    
     
                                           TABLE 9__________________________________________________________________________TWO Tower Process (FIG. 2)Exchanger Duties and Compressor Powers__________________________________________________________________________   pStream  70          71          72        73Name    WARM GAS/GAS               CHILLER DUTY                           COLD GAS/GAS                                     SUBCOOLEREnthalpy KJ/hr   611501.5000 117581.6250 848195.4375                                     84686.7656__________________________________________________________________________Stream  74          75          76        77__________________________________________________________________________Name    CONDENSER               COLD REC GAS                                     WARM REC GASEnthalpy KJ/hr   345817.3750             * 0.0000    * 204090.0781                                     204529.0469__________________________________________________________________________Stream  78          79          82        83__________________________________________________________________________Name    REC CHILLER DC2 REBOILER                           SALES COOLER                                     1ST AFTCOOLEnthalpy KJ/hr   49440.1367  147965.0000                         * 645163.4375                                     351724.7813__________________________________________________________________________Stream  84          85          86        92__________________________________________________________________________Name    2ND AFTCOOL LIQ/GAS DUTY                           COLD RES GAS                                     SALES COMPEnthalpy KJ/hr   466494.5000 195089.7813 644105.3750                                     803113.0625__________________________________________________________________________Stream  93          94          95__________________________________________________________________________Name    1ST COMPRESS               2ND COMPRESS                           C2+ PUMPEnthalpy KJ/hr   399692.8438 404052.2500 16503.7148__________________________________________________________________________ 
    
     
                                           TABLE 10__________________________________________________________________________Two Tower Process (FIG. 2)Material BalanceStream      4      37       60          9    42       33__________________________________________________________________________Name        PLANT  C2+      GASFRAC OVHD                                   ERROR                                        1ST      DC2 FEED       INLET  PRODUCT                   SUCTIONVapour frac.       1.0000 0.0000   1.0000    * --   1.0000   0.6928Temperature C.       21.0753              -65.3441                     * -89.9262  * --   32.2222                                               * -115.2480Pressure Kpa a       6294.9131              282.6850                     * 3543.9050 * --   248.2112 275.7903                                                        * -Molar                                                        Flow                                                        Kgmole/hr 297                                                        .7482 27.2160                                                         * 270.5219 *                                                         0.0103 78.81                                                        50  106.0311                                                        3Mass Flow Kg/hr       5540.7427              1081.5333                       4459.0972   0.1116                                        1361.7679                                                 2443.3013Volume Flow M3/hr       16.7591              2.3429   14.4157     0.0005                                        4.3000   6.6430Enthalpy KJ/hr       2.59635E+06              -234289.8750                       1.09745E+06 --   811394.3125                                                 20515.0625Density Kg/m3       57.4469              612.6823 69.3735     --   1.6985   7.2449Mole Wt.    18.6088              39.7388  16.4833     10.8341                                        17.2780  23.0433Spec. Heat KJ/       48.9815              83.6426  95.7635     --   37.1313  45.6116Kgmole-C.Therm Cond Watt/m-K       0.0406 0.1555   0.0310      --   0.0359   --Viscosity Cp       0.0130 0.2199   0.0093      --   0.0116   --Sur Tension Dyne/cm       --     16.8716  --          --   --       --Std Density Kg/m3       --     491.3733 --          --   --       --Z Factor    0.8335 0.0106   0.5527      --   0.9945   --N2 Kgmole/hr       5.0123 0.0000 * 5.0123    * -0.0000                                        0.0033   0.0033CO2 Kgmole/hr       3.4056 2.0041 * 1.4032    * -0.0017                                        2.0579   4.0620Methane Kgmole/hr       262.8470              0.1424 * 262.6920  * 0.0125                                        73.9797  74.1221Ethane Kgmole/hr       15.6641              14.2527                     * 1.4118    * -0.0005                                        2.7164   16.9692Propane Kgmole/hr       6.8591 6.8565 * 0.0025    * 0.0000                                        0.0562   6.9127i-Butane Kgmole/hr       1.0422 1.0422 * 0.0000    * 0.0000                                        0.0010   1.0432n-Butane Kgmole/hr       1.4193 1.4193 * 0.0000    * 0.0000                                        0.0005   1.4199i-Pentan Kgmole/hr       0.5360 0.5360 * 0.0000    * -0.0000                                        0.0000   0.5360n-Pentan Kgmole/hr       0.4764 0.4764 * 0.0000    * 0.0000                                        0.0000   0.4764n-Hexane Kgmole/hr       0.3374 0.3374 * 0.0000    * 0.0000                                        0.0000   0.3374n-Heptan Kgmole/hr       0.1488 0.1488 * 0.0000    * 0.0000                                        0.0000   0.1488Total Kgmole/hr       297.7482              27.2160                     * 270.5219  * 0.0103                                        78.8150  106.0311__________________________________________________________________________ 
    
     
                                           TABLE 11__________________________________________________________________________Two Tower Process (FIG. 2) Stream Compositions__________________________________________________________________________Stream         4        37           60__________________________________________________________________________Name           PLANT INLET                   C2+ PRODUCT  GASFRAC OVHDVapour frac.   1.0000   0.0000       1.0000    *Temperature  C.      21.0753  -65.3441   * -89.9262  *Pressure  Kpa a   6294.9131                   282.6850   * 3543.9050 *Molar Flow  Kgmole/hr          297.7482 27.2160    * 270.5219  *Mass Flow  Kg/hr   5540.7427                   1081.5333    4459.0972Volume Flow  M3/hr   16.7591  2.3429       14.4157Enthalpy  KJ/hr   2.59635E+06                   -234289.8750 1.09745E+06Density  Kg/m3   57.4469  612.6823     69.3735Mole Wt.       18.6088  39.7388      16.4833Spec. Heat  KJ/Kgmole-C.          48.9815  83.6426      95.7635Therm Cond  Watt/m-k.          0.0406   0.1555       0.0310Viscosity  Cp      0.0130   0.2199       0.0093Sur Tension  Dyne/cm --       16.8716      --Std Density  Kg/m3   --       491.3733     --Z Factor       0.8335   0.0106       0.5527N2             0.0168   0.0000     * 0.0185    *CO2            0.0114   0.0736     * 0.0052    *Methane        0.8828   0.0052     * 0.9711    *Ethane         0.0526   0.5237     * 0.0052    *Propane        0.0230   0.2519     * 0.0000    *i-Butane       0.0035   0.0383     * 0.0000    *n-Butane       0.0048   0.0522     * 0.0000    *i-Pentan       0.0018   0.0197     * 0.0000    *n-Pentan       0.0016   0.0175     * 0.0000    *n-Hexane       0.0011   0.0124     * 0.0000    *n-Heptan       0.0005   0.0055     * 0.0000    *__________________________________________________________________________Stream              42        33__________________________________________________________________________Name                1ST SUCTION                         DC2 FEEDVapour frac.        1.0000    0.6928Temperature  C.           32.2222 * -115.2480Pressure  Kpa a        248.2112  275.7903    *Molar Flow  Kgmole/hr    78.8150   106.0311Mass Flow  Kg/hr        1361.7679 2443.3013Volume Flow  M3/hr        4.3000    6.6430Enthalpy  KJ/hr        811394.3125                         20515.0625Density  Kg/m3        1.6985    7.2449Mole Wt.            17.2780   23.0433Spec. Heat  KJ/Kgmole-C. 37.1313   45.6116Therm Cond  Watt/m-k.    0.0359    --Viscosity  Cp           0.0116    --Sur Tension  Dyne/cm      --        --Std Density  Kg/m3        --        --Z Factor            0.9945    --N2                  0.0000    0.0000CO2                 0.0261    0.0383Methane             0.9386    0.6991Ethane              0.0345    0.1600Propane             0.0007    0.0652i-Butane            0.0000    0.0098n-Butane            0.0000    0.0134i-Pentan            0.0000    0.0051n-Pentan            0.0000    0.0045n-Hexane            0.0000    0.0032n-Heptan            0.0000    0.0014__________________________________________________________________________ 
    
     
                                           TABLE 12__________________________________________________________________________Two Tower Process (FIG. 2) Gas Fractionator Tower Profiles__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN10  Date 1980/1/1  Time 0:18:45COMPUTED RESULTS   Feed Conditions   Feed Stream Number              27__________________________________________________________________________   Enters on stage              5   Liquid Fraction              0.3515   Temperature              -81.15       C.   Pressure   3585.27      Kpa a   Flowrate   297.75       Kgmole/hr   Enthalpy   676020.      KJ/hr   N2         5.0123       Kgmole/hr   CO2        3.4056       Kgmole/hr   Methane    262.8470     Kgmole/hr   Ethane     15.6641      Kgmole/hr   Propane    6.8591       Kgmole/hr   i-Butane   1.0422       Kgmole/hr   n-Butane   1.4193       Kgmole/hr   i-Pentan   0.5360       Kgmole/hr   n-Pentan   0.4764       Kgmole/hr   n-Hexane   0.3374       Kgmole/hr   n-Heptan   0.1488       Kgmole/hr__________________________________________________________________________   Feed Stream Number              48__________________________________________________________________________   Enters on stage              9   Liquid Fraction              0.0000   Temperature              -34.44       C.   Pressure   3585.27      Kpa a   Flowrate   78.82        Kgmole/hr   Enthalpy   542951.      KJ/hr   N2         0.0033       Kgmole/hr   CO2        2.0579       Kgmole/hr   Methane    73.9797      Kgmole/hr   Ethane     2.7164       Kgmole/hr   Propane    0.0562       Kgmole/hr   i-Butane   0.0010       Kgmole/hr   n-Butane   0.0005       Kgmole/hr   i-Pentan   0.0000       Kgmole/hr   n-Pentan   0.0000       Kgmole/hr   n-Hexane   0.0000       Kgmole/hr   n-Heptan   0.0000       Kgmole/hr__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN10  Date 1980/1/1  Time 0:19:9Stage Variables   Press       Temp    Molar Flow Rates                               Heat DutyStage   Kpa Deg C.  Liquid                   Vapour  Feed                               GJ/Hour__________________________________________________________________________1       3543.91       -89.926  80.64                   270.52      -0.345822       3578.38       -87.934  68.91                   351.163       3579.36       -86.373  57.20                   339.434       3580.35       -84.742  40.66                   327.725       3581.33       -81.889 144.90                   311.19  297.756       3582.32       -81.291 145.37                   117.687       3583.30       -80.895 144.27                   118.148       3584.29       -80.031 138.72                   117.049       3585.27       -76.499 106.03                   111.50   78.80__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN10  Date 1980/1/1  Time 0:19:57Products    Vapour from Stage              1        Liquid from Stage                                9    Kg Mol/Hour              Mol Frc  Kg Mol/Hour                                Mol Frc__________________________________________________________________________N2       5.012     0.01853  0.003    0.00003CO2      1.403     0.00519  4.062    0.03831Methane  262.692   0.97106  74.122   0.69906Ethane   1.412     0.00522  16.969   0.16004Propane  0.003     0.00001  6.913    0.06519i-Butane 0.000     0.00000  1.043    0.00984n-Butane 0.000     0.00000  1.420    0.01339i-Pentan 0.000     0.00000  0.536    0.00506n-Pentan 0.000     0.00000  0.476    0.00449n-Hexane 0.000     0.00000  0.337    0.00318n-Heptan 0.000     0.00000  0.149    0.00140Total    270.522            106.031__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN10  Date 1980/1/1  Time 0:21:12PHYSICAL PROPERTIESVAPOUR LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M ACMH KG/M3  TEMP PRESS__________________________________________________________________________1     16.483 4459.   0.064   69.27528                              0.96083                                   0.764912     16.570 5819.   0.085   68.31509                              0.96667                                   0.770823     16.656 5654.   0.085   66.53973                              0.97173                                   0.770524     16.717 5479.   0.085   64.60286                              0.97802                                   0.770675     16.741 5210.   0.086   60.82468                              0.99228                                   0.771366     16.618 1956.   0.032   60.37632                              0.99104                                   0.769027     16.600 1961.   0.033   60.13585                              0.99123                                   0.768218     16.660 1950.   0.033   59.65896                              0.99329                                   0.767359     16.905 1885.   0.033   57.56644                              1.00401                                   0.76500__________________________________________________________________________LIQUID LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M3/HR  KG/M3  TEMP PRESS__________________________________________________________________________1     16.862 1360.   4.690  289.88832                              0.94132                                   0.758362     17.334 1195.   3.974  300.54875                              0.93466                                   0.762423     17.824 1020.   3.259  312.75522                              0.92531                                   0.760684     18.454  750.   2.289  327.77443                              0.91275                                   0.760495     20.960 3037.   7.979  380.58934                              0.86444                                   0.767126     20.932 3043.   8.027  379.01933                              0.86633                                   0.766507     21.014 3032.   7.971  380.27147                              0.86582                                   0.765848     21.384 2966.   7.660  387.20652                              0.86093                                   0.763949     23.043 2443.   5.877  415.65298                              0.83865                                   0.75982__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN10  Date 1980/1/1  Time 0:22:58TRANSPORT PROPERTIESVAPOUR                LIQUID       THERMAL          THERMAL   SURFACESTAGEVISCOSITY       CONDUCTIVITY                 VISCOSITY                        CONDUCTIVITY                                  TENSIONNO.  CP     WATT/M-K  CP     WATT/M-K  DYNE/CM__________________________________________________________________________1    0.00932       0.03103   0.03149                        0.08232   1.14612    0.00935       0.03101   0.03328                        0.08443   1.33733    0.00934       0.03082   0.03563                        0.08722   1.61584    0.00933       0.03065   0.03891                        0.09087   2.02165    0.00931       0.03043   0.05318                        0.10433   3.81526    0.00929       0.03056   0.05279                        0.10396   3.75807    0.00929       0.03059   0.05305                        0.10413   3.78418    0.00930       0.03056   0.05473                        0.10535   3.97979    0.00935       0.03040   0.06297                        0.11071   4.9228__________________________________________________________________________ 
    
     
                                           TABLE 13__________________________________________________________________________Two Tower Process (FIG. 2)Demethanizer Tower Profiles__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN10  Date 1980/1/1  Time 0:31:33COMPUTED RESULTS   Feed Conditions   Feed Stream Number              33__________________________________________________________________________   Enters on stage              1   Liquid Fraction              0.3072   Temperature              -115.25      C.   Pressure   275.79       Kpa a   Flowrate   106.03       Kgmole/hr   Enthalpy   20515.       KJ/hr   N2         0.0033       Kgmole/hr   CO2        4.0620       Kgmole/hr   Methane    74.1221      Kgmole/hr   Ethane     16.9692      Kgmole/hr   Propane    6.9127       Kgmole/hr   i-Butane   1.0432       Kgmole/hr   n-Butane   1.4199       Kgmole/hr   i-Pentan   0.5360       Kgmole/hr   n-Pentan   0.4764       Kgmole/hr   n-Hexane   0.3374       Kgmole/hr   n-Heptan   0.1488       Kgmole/hr__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN10  Date 1980/1/1  Time 0:31:36Stage Variables  Press      Temp   Molar Flow Rates    Heat DutyStage  Kpa Deg C. Liquid                 Vapour      Feed                                 GJ/Hour__________________________________________________________________________1      275.79      -115.099             32.57                 78.82       106.032      277.51      -112.244             32.61                 5.353      279.24      -100.784             33.36                 5.394      280.96       -81.242             35.45                 6.145      282.69       -65.341             27.22                 8.23            0.14795__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN10  Date 1980/1/1  Time 0:31:45Products    Vapour from Stage              1        Liquid from Stage                                5    Kg Mol/Hour              Mol Frc  Kg Mol/Hour                                Mol Frc__________________________________________________________________________N2       0.003     0.00004  0.000    0.00000CO2      2.058     0.02611  2.004    0.07363Methane  73.980    0.93865  0.142    0.00523Ethane   2.717     0.03447  14.253   0.52369Propane  0.056     0.00071  6.856    0.25193i-Butane 0.001     0.00001  1.042    0.03829n-Butane 0.001     0.00001  1.419    0.05215i-Pentan 0.000     0.00000  0.536    0.01969n-Pentan 0.000     0.00000  0.476    0.01751n-Hexane 0.000     0.00000  0.337    0.01240n-Heptan 0.000     0.00000  0.149    0.00547Total    78.816             27.216__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN10  Date 1980/1/1  Time 0:32:56PHYSICAL PROPERTIESVAPOUR LEAVING FROM EACH STAGE       FLOW           DENSITY REDUCEDSTAGE MOL WT       KG/HOUR  M ACMH                      KG/M3   TEMP                                  PRESS__________________________________________________________________________1     17.278       1362.    0.360 3.78037 0.79925                                  0.058422     17.635        94.     0.025 3.81045 0.80572                                  0.058483     19.891       107.     0.027 4.02862 0.81286                                  0.056984     27.410       168.     0.033 5.04270 0.75295                                  0.052215     33.036       272.     0.048 5.69496 0.70449                                  0.05096__________________________________________________________________________LIQUID LEAVING FROM EACH STAGE       FLOW           DENSITY REDUCEDSTAGE MOL WT       KG/HOUR  M3/HR KG/M3   TEMP                                  PRESS__________________________________________________________________________1     36.107       1176.    1.827 643.48749                              0.49752                                  0.058452     36.456       1189.    1.839 646.35817                              0.50351                                  0.058493     37.470       1250.    1.915 652.49138                              0.53028                                  0.057744     38.183       1353.    2.111 641.17559                              0.58115                                  0.057265     39.739       1082.    1.765 612.68052                              0.60963                                  0.05998__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN10  Date 1980/1/1  Time 0:34: 9TRANSPORT PROPERTIESVAPOUR                LIQUID       THERMAL          THERMAL   SURFACESTAGEVISCOSITY       CONDUCTIVITY                 VISCOSITY                        CONDUCTIVITY                                  TENSIONNO.  CP     WATT/M-K  CP     WATT/M-K  DYNE/CM__________________________________________________________________________1    0.00633       0.01831   0.36011                        0.20031   22.16702    0.00644       0.01838   0.35066                        0.19818   22.01603    0.00687       0.01815   0.31324                        0.18896   21.10764    0.00750       0.01558   0.24864                        0.17089   18.71135    0.00756       0.01391   0.21988                        0.15545   16.8712__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/1/1  Time 6:48:55Products     Vapour from Stage               1       Liquid from Stage                                10     Kg Mol/Hour               Mol Frc Kg Mol/Hour                                Mol Frc__________________________________________________________________________Hydrogen  3.915     0.00188 0.000    0.00000N2        66.831    0.03206 1.635    0.00018H2S       0.014     0.00001 0.116    0.00001CO2       1209.710  0.58039 8890.650 0.98118Methane   785.789   0.37700 130.867  0.01444Ethane    16.242    0.00779 26.700   0.00295Propane   1.798     0.00086 11.170   0.00123Total     2084.300          9061.140__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/1/1  Time 6:49:53PHYSICAL PROPERTIESVAPOUR LEAVING FROM EACH STAGE       FLOW           DENSITY REDUCEDSTAGE MOL WT       KG/HOUR  M ACMH                      KG/M3   TEMP                                  PRESS__________________________________________________________________________1     32.766       68294.   3.173 21.52612                              0.86235                                  0.174132     32.784       4432.    0.205 21.57129                              0.86185                                  0.174273     32.778       4504.    0.209 21.59811                              0.86182                                  0.174494     32.763       4553.    0.211 21.61886                              0.86185                                  0.174725     32.744       4601.    0.213 21.63665                              0.86180                                  0.174946     32.721       4657.    0.215 21.65238                              0.86159                                  0.175137     32.702       4728.    0.218 21.66941                              0.86109                                  0.175248     32.734       4839.    0.223 21.71471                              0.85983                                  0.175139     33.180       5147.    0.234 21.98564                              0.85494                                  0.1737710    36.008       6761.    0.287 23.58070                              0.83165                                  0.16612__________________________________________________________________________LIQUID LEAVING FROM EACH STAGE       FLOW           DENSITY REDUCEDSTAGE MOL WT       KG/HOUR  M3/HR KG/M3   TEMP                                  PRESS__________________________________________________________________________1     43.404       399154.  351.733                      1134.66520                              0.72913                                  0.147302     43.401       399226.  351.863                      1134.45226                              0.72924                                  0.147513     43.399       399275.  351.951                      1134.30609                              0.72932                                  0.147714     43.397       399323.  352.038                      1134.16244                              0.72939                                  0.147915     43.394       399379.  352.139                      1133.99545                              0.72947                                  0.148116     43.392       399450.  352.268                      1133.78310                              0.72958                                  0.148317     43.388       399561.  352.459                      1133.48374                              0.72976                                  0.148518     43.387       399869.  352.912                      1132.90289                              0.73027                                  0.148719     43.409       401483.  354.986                      1130.82985                              0.73279                                  0.1488610    43.562       394722.  351.868                      1121.63561                              0.74557                                  0.14874__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/1/1  Time 6:51:49TRANSPORT PROPERTIESVAPOUR                LIQUID       THERMAL          THERMAL   SURFACESTAGEVISCOSITY       CONDUCTIVITY                 VISCOSITY                        CONDUCTIVITY                                  TENSIONNO.  CP     WATT/M-K  CP     WATT/M-K  DYNE/CM__________________________________________________________________________1    0.01034       0.01892   0.20880                        0.17764   17.64352    0.01034       0.01888   0.20868                        0.17759   17.63263    0.01033       0.01888   0.20859                        0.17756   17.62534    0.01033       0.01889   0.20852                        0.17753   17.61845    0.01033       0.01890   0.20046                        0.17749   17.61056    0.01032       0.01891   0.20034                        0.17745   17.60047    0.01031       0.01893   0.20017                        0.17737   17.58478    0.01031       0.01892   0.19975                        0.17716   17.54499    0.01035       0.01876   0.19789                        0.17614   17.357910   0.01074       0.01772   0.18914                        0.17104   16.4346__________________________________________________________________________ 
    
     
                                           TABLE 14__________________________________________________________________________Three Tower Process (FIG. 3)Stream Properties__________________________________________________________________________Stream       4            9           17           18__________________________________________________________________________Name         PLANT INLET  ERROR       WARM RAW GAS COOL RAW GASVapour frac. 1.0000       --          1.0000       0.9031Temperature  F.    69.9355      --          69.9355      -57.3960Pressure  Psia  912.9997     --          912.9997     897.9997Molar Flow  Lbmole/hr        656.4217     0.0455      99.9999    * 99.9999Mass Flow  Lb/hr 12215.2314   -0.5766     1860.8795    1860.8795Volume Flow  Barrel/Day        2529.8782    0.0826      385.4040     385.4040Enthalpy  Btu/hr        2.46251E+06  --          375141.1875  179007.8281__________________________________________________________________________Stream       20           21          23           24__________________________________________________________________________Name         WARM RAW GAS COOL RAW GAS                                 CHILLED RAW  CHILLED RAWVapour frac. 1.0000       0.9861      0.9640       0.9574Temperature  F.    69.9355      -9.1004     -31.8409     -36.2363Pressure  Psia  912.9997     902.9997    897.9997     897.9997Molar Flow  Lbmole/hr        556.4218     556.4218    556.4218     656.4217Mass Flow  Lb/hr 10354.3516   10354.3516  10354.3516   12215.2314Volume Flow  Barrel/Day        2144.4741    2144.4741   2144.4741    2529.8782Enthalpy  Btu/hr        2.08736E+06  1.51253E+06 1.29993E+06  1.47894E+06__________________________________________________________________________Stream       25           26          27           30__________________________________________________________________________Name         COLD RAW GAS COLD RAW GAS                                 GAS FRAC INL GAS FRAC LIQVapour frac. 0.0000       0.7743      0.7602       0.0000    *Temperature  F.    -67.4425     -74.0000  * -107.3899    -110.4128 *Pressure  Psia  892.9997     887.9998    519.9998   * 519.9998  *Molar Flow  Lbmole/hr        656.4217     656.4217    656.4217     238.9932  *Mass Flow  Lb/hr 12215.2314   12215.2314  12215.2314   5356.3555Volume Flow  Barrel/Day        2529.8782    2529.8782   2529.8782    1015.5453Enthalpy  Btu/hr        944303.0625  850510.7500 850510.7500  -224713.2188__________________________________________________________________________Stream       31           32          33           34__________________________________________________________________________Name         SUBCOOLD LIQ ECON INLET  ECON OUTLET  CONDENSER INVapour frac. 0.0000       0.2884      0.0000       0.1630Temperature  F.    -127.4152    -178.4724   -163.5756  * -196.8716Pressure  Psia  509.9998     132.0000  * 133.0000   * 50.0000Molar Flow  Lbmole/hr        238.9932     238.9932    142.6576   * 142.6576Mass Flow  Lb/hr 5356.3555    5356.3555   4075.0251    4075.0251Volume Flow  Barrel/Day        1015.5453    1015.5453   681.8607     681.8607Enthalpy  Btu/hr        -298003.4063 -298003.4063                                 -429011.8750 -429011.8750__________________________________________________________________________Stream       35           37          38           39__________________________________________________________________________Name         DC1 FEED     C2+ LIQUID  C2+ LIQUID   C2+ LIQUIDVapour frac. 0.5103       0.0000      0.0000       0.0000Temperature  F.    -145.4947    -87.2529  * -78.6350     60.0000   *Pressure  Psia  40.0000    * 41.0000   * 899.9997   * 894.9997Molar Flow  Lbmole/hr        142.6576     63.2049   * 63.2049      63.2049Mass Flow  Lb/hr 4075.0251    2487.6819   2487.6819    2487.6819Volume Flow  Barrel/Day        681.8607     371.0230    371.0230     371.0230Enthalpy  Btu/hr        -133393.2188 -232856.2969                                 -216540.4375 -20407.1055__________________________________________________________________________Stream       4            9           17           18__________________________________________________________________________Name         PLANT INLET  ERROR       WARM RAW GAS COOL RAW GASVapour frac. 1.0000       --          1.0000       0.9031Temperature  C.    21.0753      --          21.0753      -49.6645Pressure  Kpa a 6294.9131    --          6294.9131    6191.4917Molar Flow  Kgmole/hr        297.7482     0.0207      45.3592    * 45.3592Mass Flow  Kg/hr 5540.7427    - 0.2616    844.0818     844.0818Volume Flow  M3/hr 16.7591      0.0005      2.5531       2.5531Enthalpy  KJ/hr 2.59635E+06  --          395530.7813  188737.2344__________________________________________________________________________Stream       20           21          23           24__________________________________________________________________________Name         WARM RAW GAS COOL RAW GAS                                 CHILLED RAW  CHILLED RAWVapour frac. 1.0000       0.9861      0.9640       0.9574Temperature  C.    21.0753      -22.8336    -35.4672     -37.9090Pressure  Kpa a 6294.9131    6225.9653   6191.4917    6191.4917Molar Flow  Kgmole/hr        252.3890     252.3890    252.3890     297.7482Mass Flow  Kg/hr 4696.6606    4696.6606   4696.6606    5540.7427Volume Flow  M3/hr 14.2060      14.2060     14.2060      16.7591Enthalpy  KJ/hr 2.20082E+06  1.59473E+06 1.37059E+06  1.55932E+06__________________________________________________________________________Stream       25           26          27           30__________________________________________________________________________Name         COLD RAW GAS COLD RAW GAS                                 GAS FRAC INL GAS FRAC LIQVapour frac. 0.0000       0.7743      0.7602       0.0000    *Temperature  C.    -55.2459     -58.8889  * -77.4388     -79.1182  *Pressure  Kpa a 6157.0181    6122.5444   3585.2734  * 3585.2734 *Molar Flow  Kgmole/hr        297.7482     297.7482    297.7482     108.4056  *Mass Flow  Kg/hr 5540.7427    5540.7427   5540.7427    2429.6050Volume Flow  M3/hr 16.7591      16.7591     16.7591      6.7275Enthalpy  KJ/hr 995627.6250  896737.5625 896737.5625  -236926.7813__________________________________________________________________________Stream       31           32          33           34__________________________________________________________________________Name         SUBCOOLD LIQ ECON INLET  ECON OUTLET  CONDENSER INVapour frac. 0.0000       0.2884      0.0000       0.1630Temperature  C.    -88.5640     -116.9291   -108.6531  * -127.1509Pressure  Kpa a 3516.3259    910.1079  * 917.0026   * 344.7379Molar Flow  Kgmole/hr        108.4056     108.4056    64.7085    * 64.7085Mass Flow  Kg/hr 2429.6050    2429.6050   1848.4026    1848.4026Volume Flow  M3/hr 6.7275       6.7275      4.5170       4.5170Enthalpy  KJ/hr -314200.4375 -314200.4375                                 -452329.4375 -452329.4375__________________________________________________________________________Stream       35           37          38           39__________________________________________________________________________Name         DC1 FEED     C2+ LIQUID  C2+ LIQUID   C2+ LIQUIDVapour frac. 0.5103       0.0000      0.0000       0.0000Temperature  C.    -98.6082     -66.2516  * -61.4639     15.5556   *Pressure  Kpa a 275.7903   * 282.6850  * 6205.2813  * 6170.8076Molar Flow  Kgmole/hr        64.7085      28.6693   * 28.6693      28.6693Mass Flow  Kg/hr 1848.4026    1128.3949   1128.3949    1128.3949Volume Flow  M3/hr 4.5170       2.4578      2.4578       2.4578Enthalpy  KJ/hr -140643.3750 -245512.4531                                 -228309.7969 -21516.2676__________________________________________________________________________Stream       40           41          42           43__________________________________________________________________________Name         RICH REC GAS RICH REC GAS                                 RICH REC GAS RICH REC GASVapour frac. 1.0000       1.0000      1.0000       1.0000Temperature  C.    -98.3559   * -88.7562    32.2222    * 154.8530Pressure  Kpa a 275.7903   * 262.0008    248.2112     992.8450Molar Flow  Kgmole/hr        36.0382    * 36.0382     36.0382      36.0382Mass Flow  Kg/hr 720.5903     720.5903    720.5903     720.5903Volume Flow  M3/hr 2.0596       2.0596      2.0596       2.0596Enthalpy  KJ/hr 204204.8438  216567.0000 375997.0938  558298.7500__________________________________________________________________________Stream       44           47          48           50__________________________________________________________________________Name         RICH REC GAS RICH REC GAS                                 ECON INLET   LEAN REC GASVapour frac. 1.0000       1.0000      1.0000       1.0000Temperature  C.    51.6667    * -63.2283    -63.5434     -116.6819 *Pressure  Kpa a 972.1607     944.5817    917.0026   * 910.1079  *Molar Flow  Kgmole/hr        36.0382      36.0382     36.0382      79.7354   *Mass Flow  Kg/hr 720.5903     720.5903    720.5903     1301.7927Volume Flow  M3/hr 2.0596       2.0596      2.0596       4.2701Enthalpy  KJ/hr 398264.5313  238834.4531 238834.4531  376987.2500__________________________________________________________________________Stream       51           52          53           54__________________________________________________________________________Name         LEAN REC GAS LEAN REC GAS                                 LEAN REC GAS LEAN REC GASVapour frac. 1.0000       1.0000      1.0000       1.0000Temperature  C.    -88.7562     32.2222   * 172.1851     43.3333   *Pressure  Kpa a 889.4236     868.7394    3730.0637    3702.4846Molar Flow  Kgmole/hr        79.7354      79.7354     79.7354      79.7354Mass Flow  Kg/hr 1301.7927    1301.7927   1301.7927    1301.7927Volume Flow  M3/hr 4.2701       4.2701      4.2701       4.2701Enthalpy  KJ/hr 460240.8438  807988.8125 1.23575E+06  803972.8750__________________________________________________________________________Stream       55           56          57           58__________________________________________________________________________Name         LEAN REC GAS LEAN REC GAS                                 LEAN REC GAS LEAN REC GASVapour frac. 1.0000       1.0000      1.0000       0.7506Temperature  C.    -61.0147     -61.2540    -85.9784     -89.9250Pressure  Kpa a 3674.9055    3647.3264   3612.8525    3578.3787 *Molar Flow  Kgmole/hr        79.7354      79.7354     79.7354      79.7354Mass Flow  Kg/hr 1301.7927    1301.7927   1301.7927    1301.7927Volume Flow  M3/hr 4.2701       4.2701      4.2701       4.2701Enthalpy  KJ/hr 456224.9063  456224.9063 342542.8438  246927.0625__________________________________________________________________________Stream       60           61          62           63__________________________________________________________________________Name         RESIDUE GAS  RESIDUE GAS RESIDUE GAS  RESIDUE GASVapour frac. 1.0000     * 1.0000      1.0000       1.0000Temperature  C.    -91.3418   * -88.7562    -83.0648     -40.0000  *Pressure  Kpa a 3537.0103  * 3509.4312   3481.8521    3447.3782Molar Flow  Kgmole/hr        269.0583   * 269.0583    269.0583     269.0583Mass Flow  Kg/hr 4412.6094    4412.6094   4412.6094    4412.6094Volume Flow  M3/hr 14.3007      14.3007     14.3007      14.3007Enthalpy  KJ/hr 1.06364E+06  1.14091E+06 1.25460E+06  1.81830E+06__________________________________________________________________________Stream       64           66          68__________________________________________________________________________Name         RESIDUE GAS  RESIDUE GAS RESIDUE GASVapour frac. 1.0000       1.0000      1.0000Temperature  C.    15.5556    * 103.2331    48.8889    *Pressure  Kpa a 3412.9043    8397.8135   8363.3398  *Molar Flow  Kgmole/hr        269.0583     269.0583    269.0583Mass Flow  Kg/hr 4412.6094    4412.6094   4412.6094Volume Flow  M3/hr 14.3007      14.3007     14.3007Enthalpy  KJ/hr 2.42438E+06  3.22616E+06 2.58199E+06__________________________________________________________________________ 
    
     
                                           TABLE 15__________________________________________________________________________THREE Tower Process (FIG. 3)Exchanger Duties and Compressor Power__________________________________________________________________________Stream   70          71        73          74__________________________________________________________________________Name     WARM GAS/GAS                RAW CHILLER                          SUBCOOLER   CONDENSEREnthalpyKJ/hr    606083.2500 224148.2188                          77273.6406  311686.0625                                                *__________________________________________________________________________Stream   75          76        77          78__________________________________________________________________________Name     CRYOGEN CHIL                COLD RICH RG                          WARM RICH RG                                      RICH CHILLEREnthalpyKJ/hr    113682.0703 12362.1523                          159430.0781 0.0000    *__________________________________________________________________________Stream   79          82        83          84__________________________________________________________________________Name     DC1 REBOILER                SALES COOLER                          RICH COOLER LEAN COOLEREnthalpyKJ/hr    98890.0703              * 644174.8750                          160034.2188 431783.6250__________________________________________________________________________Stream   85          86        87          92__________________________________________________________________________Name     LIQ/GAS DUTY                COLD GAS/GAS                          RICH CHILLER                                      SALES COMPEnthalpyKJ/hr    206793.5313 563700.3125                          0.0000    * 801782.8125__________________________________________________________________________Stream   93          94        95          96__________________________________________________________________________Name     RICH REC COM                LEAN REC COM                          C2+ PUMP    COLD LEAN RGEnthalpyKJ/hr    182301.6563 427767.7188                          17202.6504  83253.6094__________________________________________________________________________Stream   97          98__________________________________________________________________________Name     WARM LEAN RG                CRYOGEN CONDEnthalpyKJ/hr    347748.0000 95615.7656__________________________________________________________________________ 
    
     
                                           TABLE 16__________________________________________________________________________Three Tower Process (FIG. 3)Material Balance__________________________________________________________________________Stream         4          37          60         9__________________________________________________________________________Name           PLANT INLET                     C2+ LIQUID  RESIDUE GAS                                            ERRORVapour frac.   1.0000     0.0000      1.0000   * --Temperature  C.      21.0753    -66.2516  * -91.3418 * --Pressure  Kpa a   6294.9131  282.6850  * 3537.0103                                          * --Molar Flow  Kgmole/hr          297.7482   28.6693   * 269.0583 * 0.0207Mass Flow  Kg/hr   5540.7427  1128.3949   4412.6094  -0.2616Volume Flow  M3/hr   16.7591    2.4578      14.3007    0.0005Enthalpy  KJ/hr   2.59635E+06                     -245512.4531                                 1.06364E+06                                            --Density  Kg/m3   57.4469    613.1561    71.2335    --Mole Wt.       18.6088    39.3590     16.4002    -12.6599Spec. Heat  KJ/Kgmole-C.          48.9815    82.9568     103.8304   --Therm Cond  Watt/m-K.          0.0406     0.1561      0.0313     --Viscosity  Cp      0.0130     0.2184      0.0093     --Sur Tension  Dyne/cm --         16.8615     --         --Std Density  Kg/m3   --         488.8882    --         --Z Factor       0.8335     0.0105      0.5387     --N2     Kgmole/hr          5.0123     0.0000    * 5.0122   * 0.0002CO2    Kgmole/hr          3.4056     2.2396    * 1.1779   * -0.0118Methane  Kgmole/hr          262.8470   0.1543    * 262.6423 * 0.0504Ethane Kgmole/hr          15.6641    15.4553   * 0.2259   * -0.0172Propane  Kgmole/hr          6.8591     6.8598    * 0.0000   * -0.0008i-Butane  Kgmole/hr          1.0422     1.0422    * 0.0000   * -0.0000n-Butane  Kgmole/hr          1.4193     1.4193    * 0.0000   * -0.0000i-Pentan  Kgmole/hr          0.5360     0.5360    * 0.0000   * -0.0000n-Pentan  Kgmole/hr          0.4764     0.4764    * 0.0000   * -0.0000n-Hexane  Kgmole/hr          0.3374     0.3374    * 0.0000   * -0.0000n-Heptan  Kgmole/hr          0.1488     0.1488    * 0.0000   * 0.0000Total  Kgmole/hr          297.7482   28.6693   * 269.0583 * 0.0207__________________________________________________________________________Stream         48         58          32         35__________________________________________________________________________Name           ECON INLET LEAN REC GAS                                 ECON INLET DC1 FEEDVapour frac.   1.0000     0.7506      0.2884     0.5103Temperature  C.      -63.5434   -89.9250    -116.9291  -98.6082Pressure  Kpa a   917.0026 * 3578.3787 * 910.1079 * 275.7903                                                   *Molar Flow  Kgmole/hr          36.0382    79.7354     108.4056   64.7085Mass Flow  Kg/hr   720.5903   1301.7927   2429.6050  1848.4026Volume Flow  M3/hr   2.0596     4.2701      6.7275     4.5170Enthalpy  KJ/hr   238834.4531                     246927.0625 -314200.4375                                            -140643.3750Density  Kg/m3   11.4031    87.2113     57.6247    10.9260Mole Wt.       19.9952    16.3264     22.4122    28.5651Spec. Heat  KJ/Kgmole-C.          37.5708    115.2043    56.6370    54.3779Therm Cond  Watt/m-K.          0.0231     --          --         --Viscosity  Cp      0.0084     --          --         --Sur Tension  Dyne/cm --         --          --         --Std Density  Kg/m3   --         --          --         --Z Factor       0.9226     --          --         --N2     Kgmole/hr          0.0002     0.4903      0.4903     0.0002CO2    Kgmole/hr          2.8730     0.3416      2.5692     5.1006Methane  Kgmole/hr          28.8661    78.4042     78.5895    29.0513Ethane Kgmole/hr          4.1770     0.4872      15.9253    19.6151Propane  Kgmole/hr          0.1174     0.0116      6.8706     6.9764i-Butane  Kgmole/hr          0.0027     0.0002      1.0424     1.0449n-Butane  Kgmole/hr          0.0016     0.0001      1.4195     1.4210i-Pentan  Kgmole/hr          0.0001     0.0000      0.5360     0.5361n-Pentan  Kgmole/hr          0.0000     0.0000      0.4764     0.4765n-Hexane  Kgmole/hr          0.0000     0.0000      0.3374     0.3374n-Heptan  Kgmole/hr          0.0000     0.0000      0.1488     0.1488Total  Kgmole/hr          36.0382    79.7354     108.4056   64.7085__________________________________________________________________________ 
    
     
                                           TABLE 17__________________________________________________________________________Three Tower Process (FIG. 3)Stream Compositions__________________________________________________________________________Stream              4        37          60__________________________________________________________________________Name                PLANT INLET                        C2+ LIQUID  RESIDUE GASVapour frac.        1.0000   0.0000      1.0000     *Temperature     C.        21.0753  -66.2516  * -91.3418   *Pressure  Kpa a     6294.9131                        282.6850  * 3537.0103  *Molar Flow     Kgmole/hr 297.7482 28.6693   * 269.0583   *Mass Flow Kg/hr     5540.7427                        1128.3949   4412.6094Volume Flow     M3/hr     16.7591  2.4578      14.3007Enthalpy  KJ/hr     2.59635E+06                        -245512.4531                                    1.06364E+06Density   Kg/m3     57.4469  613.1561    71.2335Mole Wt.            18.6088  39.3590     16.4002Spec. Heat     KJ/Kgmole-C.               48.9815  82.9568     103.8304Therm Cond     Watt/m-K. 0.0406   0.1561      0.0313Viscosity Cp        0.0130   0.2184      0.0093Sur Tension     Dyne/cm   --       16.8615     --Std Density     Kg/m3     --       488.8882    --Z Factor            0.8335   0.0105      0.5387N2                  0.0168   0.0000    * 0.0186     *CO2                 0.0114   0.0781    * 0.0044     *Methane             0.8828   0.0054    * 0.9762     *Ethane              0.0526   0.5391    * 0.0008     *Propane             0.0230   0.2393    * 0.0000     *i-Butane            0.0035   0.0364    * 0.0000     *n-Butane            0.0048   0.0495    * 0.0000     *i-Pentan            0.0018   0.0187    * 0.0000     *n-Pentan            0.0016   0.0166    * 0.0000     *n-Hexane            0.0011   0.0118    * 0.0000     *n-Heptan            0.0005   0.0052    * 0.0000     *__________________________________________________________________________Stream         48        58          32        35__________________________________________________________________________Name           ECON INLET                    LEAN REC GAS                                ECON INLET                                          DC1 FEEDVapour frac.   1.0000    0.7506      0.2884    0.5103Temperature  C.      -63.5434  -89.9250    -116.9291 -98.6082Pressure  Kpa a   917.0026                  * 3578.3787 * 910.1079                                        * 275.7903                                                 *Molar Flow  Kgmole/hr          36.0382   79.7354     108.4056  64.7085Mass Flow  Kg/hr   720.5903  1301.7927   2429.6050 1848.4026Volume Flow  M3/hr   2.0596    4.2701      6.7275    4.5170Enthalpy  KJ/hr   238834.4531                    246927.0625 -314200.4375                                          -140643.3750Density  Kg/m3   11.4031   87.2113     57.6247   10.9260Mole Wt.       19.9952   16.3264     22.4122   28.5651Spec. Heat  KJ/Kgmole-C.          37.5708   115.2043    56.6370   54.3779Therm Cond  Watt/m-K.          0.0231    --          --        --Viscosity  Cp      0.0084    --          --        --Sur Tension  Dyne/cm --        --          --        --Std Density  Kg/m3   --        --          --        --Z Factor       0.9226    --          --        --N2             0.0000    0.0061      0.0045    0.0000CO2            0.0797    0.0043      0.0237    0.0788Methane        0.8010    0.9833      0.7250    0.4490Ethane         0.1159    0.0061      0.1469    0.3031Propane        0.0033    0.0001      0.0634    0.1078i-Butane       0.0001    0.0000      0.0096    0.0161n-Butane       0.0000    0.0000      0.0131    0.0220i-Pentan       0.0000    0.0000      0.0049    0.0083n-Pentan       0.0000    0.0000      0.0044    0.0074n-Hexane       0.0000    0.0000      0.0031    0.0052n-Heptan       0.0000    0.0000      0.0014    0.0023__________________________________________________________________________ 
    
     
                                           TABLE 18__________________________________________________________________________Three Tower Process (FIG. 3)Gas Fractionator Tower Profiles__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30  Date 1980/ 1/ 1  Time 1:32:53COMPUTED RESULTS         Feed Conditions         Feed Stream Number      58__________________________________________________________________________         Enters on stage         4         Liquid Fraction         0.2494         Temperature             -89.92                                      C.         Pressure                3578.38                                      Kpa a         Flowrate                79.74                                      Kgmole/hr         Enthalpy                246927.                                      KJ/hr         N2                      0.4903                                      Kgmole/hr         CO2                     0.3416                                      Kgmole/hr         Methane                 78.4042                                      Kgmole/hr         Ethane                  0.4872                                      Kgmole/hr         Propane                 0.0116                                      Kgmole/hr         i-Butane                0.0002                                      Kgmole/hr         n-Butane                0.0001                                      Kgmole/hr         i-Pentan                0.0000                                      Kgmole/hr         n-Pentan                0.0000                                      Kgmole/hr         n-Hexane                0.0000                                      Kgmole/hr         n-Heptan                0.0000                                      Kgmole/hr__________________________________________________________________________         Feed Stream Number      27__________________________________________________________________________         Enters on stage         12         Liquid Fraction         0.2398         Temperature             -77.44                                      C.         Pressure                3585.27                                      Kpa a         Flowrate                297.75                                      Kgmole/hr         Enthalpy                896738.                                      KJ/hr         N2                      5.0123                                      Kgmole/hr         CO2                     3.4056                                      Kgmole/hr         Methane                 262.8470                                      Kgmole/hr         Ethane                  15.6641                                      Kgmole/hr         Propane                 6.8591                                      Kgmole/hr         i-Butane                1.0422                                      Kgmole/hr         n-Butane                1.4193                                      Kgmole/hr         i-Pentan                0.5360                                      Kgmole/hr         n-Pentan                0.4764                                      Kgmole/hr         n-Hexane                0.3374                                      Kgmole/hr         n-Heptan                0.1488                                      Kgmole/hr__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30  Date 1980/ 1/ 1  Time 1:33:17Stage Variables      Press          Temp       Molar Flow Rates         Heat DutyStage      Kpa Deg C.     Liquid                         Vapour           Feed                                              GJ/Hour__________________________________________________________________________1          3537.01          -91.342    84.11                         269.06               -0.311692          3541.40          -90.810    81.10                         353.173          3545.79          -90.437    78.50                         350.164          3550.17          -90.111    95.60                         347.56            79.725          3554.56          -89.690    91.25                         284.946          3558.95          -89.095    86.38                         280.597          3563.34          -88.357    80.78                         275.728          3567.72          -87.442    74.41                         270.129          3572.11          -86.316    67.34                         263.7510         3576.50          -84.945    59.04                         256.6911         3580.89          -83.151    43.63                         248.3812         3585.27          -79.118    108.41                         232.97           297.75__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30  Date 1980/ 1/ 1  Time 1:34:16Products         Vapour from Stage                   1              Liquid from Stage                                           12         Kg Mol/Hour                   Mol Frc        Kg Mol/Hour                                           Mol Frc__________________________________________________________________________N2            5.012     0.01863        0.490    0.00452CO2           1.178     0.00438        2.569    0.02370Methane       262.642   0.97615        78.589   0.72496Ethane        0.226     0.00084        15.925   0.14691Propane       0.000     0.00000        6.871    0.06338i-Butane      0.000     0.00000        1.042    0.00962n-Butane      0.000     0.00000        1.419    0.01309i-Pentan      0.000     0.00000        0.536    0.00494n-Pentan      0.000     0.00000        0.476    0.00439n-Hexane      0.000     0.00000        0.337    0.00311n-Heptan      0.000     0.00000        0.149    0.00137Total         269.058                  108.406__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30  Date 1980/ 1/ 1  Time 1:35:34PHYSICAL PROPERTIES     VAPOUR LEAVING FROM EACH STAGE           FLOW                DENSITY     REDUCEDSTAGE     MOL WT           KG/HOUR       M ACMH                               KG/M3       TEMP                                               PRESS__________________________________________________________________________1         16.400           4413.         0.062 70.92639    0.95642                                               0.763982         16.423           5800.         0.082 70.55957    0.95713                                               0.763713         16.455           5762.         0.082 70.29640    0.95810                                               0.764204         16.478           5727.         0.082 70.05559    0.95911                                               0.764935         16.567           4720.         0.068 69.80972    0.96048                                               0.765496         16.631           4666.         0.067 69.33809    0.96212                                               0.765827         16.689           4602.         0.067 68.67073    0.96432                                               0.766278         16.746           4523.         0.067 67.79028    0.96723                                               0.766899         16.801           4431.         0.066 66.68371    0.97102                                               0.7677010        16.855           4327.         0.066 65.33570    0.97590                                               0.7687211        16.904           4199.         0.066 63.48810    0.98301                                               0.7700212        16.919           3942.         0.067 58.82507    1.00336                                               0.77205__________________________________________________________________________     LIQUID LEAVING FROM EACH STAGE           FLOW                DENSITY     REDUCEDSTAGE     MOL WT           KG/HOUR       M3/HR KG/M3       TEMP                                               PRESS__________________________________________________________________________1         16.495           1387.         4.946 280.47753   0.94774                                               0.758882         16.635           1349.         4.753 283.79282   0.94608                                               0.757763         16.746           1315.         4.589 286.45455   0.94466                                               0.757554         16.835           1609.         5.576 288.57886   0.94342                                               0.757825         17.044           1555.         5.290 293.94449   0.94056                                               0.756616         17.254           1490.         4.980 299.21650   0.93752                                               0.755547         17.483           1412.         4.631 304.92027   0.93387                                               0.754748         17.744           1320.         4.240 311.33508   0.92930                                               0.754289         18.047           1215.         3.814 318.62769   0.92354                                               0.7542110        18.420           1087.         3.323 327.23580   0.91610                                               0.7546811        19.037            830.         2.436 340.92432   0.90359                                               0.7561912        22.412           2430.         5.990 405.54499   0.84179                                               0.76752__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30  Date 1980/ 1/ 1  Time 1:37:50TRANSPORT PROPERTIES  VAPOUR                            LIQUID              THERMAL               THERMAL   SURFACESTAGE  VISCOSITY   CONDUCTIVITY                        VISCOSITY   CONDUCTIVITY                                              TENSIONNO.    CP          WATT/M-K  CP          WATT/M-K  DYNE/CM__________________________________________________________________________1      0.00933     0.03122   0.02989     0.08024   0.97222      0.00933     0.03120   0.03030     0.08080   1.01243      0.00933     0.03117   0.03066     0.08127   1.04844      0.00933     0.03115   0.03098     0.08167   1.08155      0.00934     0.03105   0.03165     0.08253   1.15236      0.00934     0.03098   0.03239     0.08348   1.23297      0.00934     0.03090   0.03331     0.08461   1.33528      0.00934     0.03080   0.03448     0.08599   1.46999      0.00935     0.03070   0.03598     0.08769   1.647610     0.00935     0.03059   0.03794     0.08981   1.887811     0.00935     0.03047   0.04134     0.09330   2.314912     0.00934     0.03026   0.06103     0.10972   4.7372__________________________________________________________________________Molar Flow  Kgmole/hr        63.4545      52.7218   *  0.7296   *  10.7296Mass Flow  Kg/hr 3008.2058    2040.1130    67.9293     967.9293Volume Flow  M3/hr 5.7646       4.3169       1.4473      1.4473Enthalpy  KJ/hr -30736.5313  793143.3750  295021.2188 -12811.6641__________________________________________________________________________Stream       39__________________________________________________________________________Name         C5+ REID VPVapour frac. 0.0000    *Temperature  C.    37.7778   *Pressure  Kpa a 81.1159Molar Flow  Kgmole/hr        10.7296Mass Flow  Kg/hr 967.9293Volume Flow  M3/hr 1.4473Enthalpy  KJ/hr -12811.6641__________________________________________________________________________Stream       40           41           42          43__________________________________________________________________________Name         LOW TEMP GAS DEHY OUTLETVapour frac. 1.0000       1.0000       0.9311      0.8641Temperature  C.    -8.6641      -8.7406      -37.0000 *  -51.5500Pressure  Kpa a 3880.0000    3870.0000 *  3835.0000   3800.0000Molar Flow  Kgmole/hr        608.9576     608.9576     608.9576    608.9576Mass Flow  Kg/hr 11813.7881   11813.7881   11813.7881  11813.7881Volume Flow  M3/hr 35.4232      35.4232      35.4232     35.4232Enthalpy  KJ/hr 4.84553E+06  4.84553E+06  3.59587E+06 2.83075E+06__________________________________________________________________________Stream       44           50           51          52__________________________________________________________________________Name         GAS FRAC IN  GAS FRAC LIQ GAS FRAC LIQ                                              GAS FRAC LIQVapour frac. 0.8650       0.0000       0.0000      0.4008Temperature  C.    -52.9688     -53.1752  *  -68.2282    -109.1413Pressure  Kpa a 3600.0000 *  3600.0000 *  3550.0000   175.0000Molar Flow  Kgmole/hr        608.9576     102.4116  *  102.4116    102.4116Mass Flow  Kg/hr 11813.7881   3111.9280    3111.9280   3111.9280Volume Flow  M3/hr 35.4232      7.5570       7.5570      7.5570Enthalpy  KJ/hr 2.83075E+06  -404555.0625 -526802.1250                                              -526802.1250__________________________________________________________________________Stream       53           54           55          56__________________________________________________________________________Name         DC2 FEED     DC2 OVERHEAD             DC2 RECYCLEVapour frac. 0.6780       1.0000    *  1.0000      1.0000Temperature  C.    -71.2590     -70.7176  *  -40.0000 *  35.0000  *Pressure  Kpa a 140.0000  *  140.0000  *  130.0000    120.0000Molar Flow  Kgmole/hr        102.4116     71.8124   *  71.8124     71.8124Mass Flow  Kg/hr 3111.9280    1670.0835    1670.0835   1670.0835Volume Flow  M3/hr 7.5570       4.7552       4.7552      4.7552Enthalpy  KJ/hr 116865.1797  505050.1250  593723.0000 827100.1875__________________________________________________________________________Stream       57           58           59          60__________________________________________________________________________Name         LPG PRODUCT  LPG PRODUCT  LPG PRODUCT LPG REID VPVapour frac. 0.0001       0.0000       0.0000      0.0000   *Temperature  C.    -43.8084  *  -42.6757     37.7988     37.7778  *Pressure  Kpa a 147.0000  *  1520.0000    1470.0000                                           *  1397.7695Molar Flow  Kgmole/hr        30.5992   *  30.5992      30.5992     30.5992Mass Flow  Kg/hr 1441.8444    1441.8444    1441.8444   1441.8444Volume Flow  M3/hr 2.8018       2.8018       2.8018      2.8018Enthalpy  KJ/hr -274486.0313 -269300.9688 11026.9502  11026.9502__________________________________________________________________________Stream       61           62           63          64__________________________________________________________________________Name         RESIDUE GAS  RESIDUE GAS  RESIDUE GASVapour frac. 0.9999       1.0000       1.0000      1.0000Temperature  C.    -71.2282  *  -67.2484     -40.0000 *  35.0000  *Pressure  Kpa a 3550.0000 *  3525.0000    3490.0000   3455.0000Molar Flow  Kgmole/hr        506.5427  *  506.5427     506.5427    506.5427Mass Flow  Kg/hr 8701.7588    8701.7588    8701.7588   8701.7588Volume Flow  M3/hr 27.8659      27.8659      27.8659     27.8659Enthalpy  KJ/hr 2.59148E+06  2.71373E+06  3.39018E+06 4.98767E+06__________________________________________________________________________Stream       65           66           67__________________________________________________________________________Name         O SUCTION    3RD DISCHARG LES GASVapour frac. 1.0000       1.0000       1.0000Temperature  C.    35.0000      121.9936     48.0000  *Pressure  Kpa a 3455.0000    8388.3398 *  8353.3398Molar Flow  Kgmole/hr        494.5427     494.5427     494.5427Mass Flow  Kg/hr 8495.6143    8495.6143    8495.6143Volume Flow  M3/hr 27.2058      27.2058      27.2058Enthalpy  KJ/hr 4.86951E+06  6.41811E+06  4.72939E+06__________________________________________________________________________ 
    
     
                                           TABLE 19__________________________________________________________________________Three Tower Process (FIG. 3)__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30 Date 1980/1/1 Time 1:43:38COMPUTED RESULTS   Feed Conditions   Feed Stream Number 32__________________________________________________________________________   Enters on stage    1   Liquid Fraction    0.7116   Temperature        -116.93                           C   Pressure           910.11                           Kpa a   Flowrate           108.41                           Kgmole/hr   Enthalpy           -314200.                           KJ/hr   N2                 0.4903                           Kgmole/hr   CO2                2.5692                           Kgmole/hr   Methane            78.5895                           Kgmole/hr   Ethane             15.9253                           Kgmole/hr   Propane            6.8706                           Kgmole/hr   i-Butane           1.0424                           Kgmole/hr   n-Butane           1.4195                           Kgmole/hr   i-Pentan           0.5360                           Kgmole/hr   n-Pentan           0.4764                           Kgmole/hr   n-Hexane           0.3374                           Kgmole/hr   n-Heptan           0.1488                           Kgmole/hr__________________________________________________________________________   Feed Stream Number 48__________________________________________________________________________   Enters on stage    3   Liquid Fraction    0.0000   Temperature        -63.54                           C   Pressure           917.00                           Kpa a   Flowrate           36.04                           Kgmole/hr   Enthalpy           238834.                           KJ/hr   N2                 0.0002                           Kgmole/hr   CO2                2.8730                           Kgmole/hr   Methane            28.8661                           Kgmole/hr   Ethane             4.1770                           Kgmole/hr   Propane            0.1174                           Kgmole/hr   i-Butane           0.0027                           Kgmole/hr   n-Butane           0.0016                           Kgmole/hr   i-Pentan           0.0001                           Kgmole/hr   n-Pentan           0.0000                           Kgmole/hr   n-Hexane           0.0000                           Kgmole/hr   n-Heptan           0.0000                           Kgmole/hr__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30 Date 1980/1/1 Time 1:44:0Stage Variables   Press       Temp    Molar Flow Rates                               Heat DutyStage   Kpa Deg C.  Liquid                   Vapour   Feed                               GJ/Hour__________________________________________________________________________1       910.11       -116.682               77.03                   79.74    108.412       913.56       -115.721               75.09                   48.363       917.00       -108.653               64.71                   46.42     36.04__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30 Date 1980/1/1 Time 1:44:28Products    Vapour from Stage              1        Liquid from Stage                                3    Kg Mol/Hour              Mol Frc  Kg Mol/Hour                                Mol Frc__________________________________________________________________________N2       0.490     0.00615  0.000    0.00000CO2      0.342     0.00428  5.101    0.07882Methane  78.404    0.98331  29.051   0.44896Ethane   0.487     0.00611  19.615   0.30313Propane  0.012     0.00015  6.976    0.10781i-Butane 0.000     0.00000  1.045    0.01615n-Butane 0.000     0.00000  1.421    0.02196i-Pentan 0.000     0.00000  0.536    0.00828n-Pentan 0.000     0.00000  0.476    0.00736n-Hexane 0.000     0.00000  0.337    0.00521n-Heptan 0.000     0.00000  0.149    0.00230Total    79.735             64.708__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30 Date 1980/1/1 Time 1:45:39PHYSICAL PROPERTIESVAPOUR LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M ACMH KG/M3  TEMP PRESS__________________________________________________________________________1     16.326 1302.   0.098   13.26088                              0.81699                                   0.195882     16.300  788.   0.060   13.19365                              0.81963                                   0.196203     16.673  774.   0.061   12.76733                              0.84739                                   0.19575__________________________________________________________________________LIQUID LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M3/HR  KG/M3  TEMP PRESS__________________________________________________________________________1     24.875 1916.   3.723  514.63485                              0.63418                                   0.194152     25.327 1902.   3.645  521.70944                              0.63123                                   0.194123     28.565 1848.   3.254  567.91168                              0.61117                                   0.19017__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30 Date 1980/1/1 Time 1:46:33TRANSPORT PROPERTIESVAPOUR                LIQUID       THERMAL          THERMAL   SURFACESTAGEVISCOSITY       CONDUCTIVITY                 VISCOSITY                        CONDUCTIVITY                                  TENSIONNO.  CP     WATT/M-K  CP     WATT/M-K  DYNE/CM__________________________________________________________________________1    0.00652       0.02041   0.14018                        0.16750   13.14102    0.00654       0.02050   0.14398                        0.16840   13.39903    0.00679       0.02093   0.17315                        0.17365   15.2267__________________________________________________________________________ 
    
     
                                           TABLE 20__________________________________________________________________________Three TowerPProcess (FIG. 3)Demethanizer Tower Profiles__________________________________________________________________________      I don&#39;t understand TABLE in the current context      type ? or ?? for more information      I don&#39;t understand 20: in the current context      type ? or ?? for more information      I don&#39;t understand THREE in the current context      type ? or ?? for more information      I don&#39;t understand TOWER in the current context      type ? or ?? for more information      I don&#39;t understand PROCESS in the current context      type ? or ?? for more information      I don&#39;t understand (FIGURE in the current context      type ? or ?? for more information      Enter a COLUMN command__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30 Date 1980/1/1 Time 0:9:2COMPUTED RESULTS   Feed Conditions   Feed Stream Number 35__________________________________________________________________________   Enters on stage    1   Liquid Fraction    0.4897   Temperature        -98.61                           C   Pressure           275.79                           Kpa a   Flowrate           64.71                           Kgmole/hr   Enthalpy           -140643.                           KJ/hr   N2                 0.0002                           Kgmole/hr   CO2                5.1006                           Kgmole/hr   Methane            29.0513                           Kgmole/hr   Ethane             19.6151                           Kgmole/hr   Propane            6.9764                           Kgmole/hr   i-Butane           1.0449                           Kgmole/hr   n-Butane           1.4210                           Kgmole/hr   i-Pentan           0.5361                           Kgmole/hr   n-Pentan           0.4765                           Kgmole/hr   n-Hexane           0.3374                           Kgmole/hr   n-Heptan           0.1488                           Kgmole/hr__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30 Date 1980/1/1 Time 0:9:5Stage Variables   Press       Temp    Molar Flow Rates                               Heat DutyStage   Kpa Deg C.  Liquid                   Vapour   Feed                               GJ/Hour__________________________________________________________________________1       275.79       -98.356 31.69                   36.04    64.712       277.51       -95.907 31.93                   3.023       279.24       -88.811 32.72                   3.264       280.96       -77.548 34.10                   4.055       282.69       -66.252 28.67                   5.43        0.09889__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30 Date 1980/1/1 Time 0:9:14Products    Vapour from Stage              1        Liquid from Stage                                5    Kg Mol/Hour              Mol Frc  Kg Mol/Hour                                Mol Frc__________________________________________________________________________N2       0.000     0.00001  0.000    0.00000CO2      2.873     0.07972  2.240    0.07812Methane  28.866    0.80098  0.154    0.00538Ethane   4.177     0.11591  15.455   0.53909Propane  0.117     0.00326  6.860    0.23927i-Butane 0.003     0.00008  1.042    0.03635n-Butane 0.002     0.00005  1.419    0.04951i-Pentan 0.000     0.00000  0.536    0.01870n-Pentan 0.000     0.00000  0.476    0.01662n-Hexane 0.000     0.00000  0.337    0.01177n-Heptan 0.000     0.00000  0.149    0.00519Total    36.038             28.669__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30 Date 1980/1/1 Time 0:10:25PHYSICAL PROPERTIESVAPOUR LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M ACMH KG/M3  TEMP PRESS__________________________________________________________________________1     19.995  721.   0.183   3.94039                              0.81810                                   0.056442     20.699  62.    0.015   4.04915                              0.81456                                   0.056263     23.300  76.    0.017   4.41685                              0.79397                                   0.054714     28.892  117.   0.022   5.22470                              0.73927                                   0.051575     33.058  180.   0.031   5.72511                              0.70225                                   0.05080__________________________________________________________________________LIQUID LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M3/HR  KG/M3  TEMP PRESS__________________________________________________________________________1     37.582 1191.   1.860  640.20737                              0.53377                                   0.057932     37.720 1204.   1.880  640.67459                              0.54017                                   0.058073     38.064 1245.   1.943  640.84708                              0.55891                                   0.057824     38.355 1308.   2.064  633.55958                              0.58924                                   0.057655     39.359 1128.   1.840  613.15855                              0.61026                                   0.05961__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name MACUN30 Date 1980/1/1 Time 0:11:37TRANSPORT PROPERTIESVAPOUR                LIQUID       THERMAL          THERMAL   SURFACESTAGEVISCOSITY       CONDUCTIVITY                 VISCOSITY                        CONDUCTIVITY                                  TENSIONNO.  CP     WATT/M-K  CP     WATT/M-K  DYNE/CM__________________________________________________________________________1    0.00692       0.01821   0.30530                        0.18516   20.67292    0.00701       0.01803   0.29688                        0.18312   20.42053    0.00726       0.01716   0.27372                        0.17714   19.64454    0.00755       0.01508   0.23929                        0.16701   18.19995    0.00755       0.01385   0.21838                        0.15611   16.8615__________________________________________________________________________ 
    
     
                                           TABLE 21__________________________________________________________________________Treating Natural Gas Containing Asphaltenes (FIG. 4) Stream__________________________________________________________________________PropertiesStream       5          9           14         15__________________________________________________________________________Name         FUEL GAS   ERRORVapour frac. 1.0000     --          1.0000     0.9967Temperature  C.    35.0000    --          45.0000    17.9363Pressure  Kpa a 3455.0000  --          3950.0000  3920.0000Molar Flow  Kgmole/hr        12.0000  * 0.0064      200.0000 * 200.0000Mass Flow  Kg/hr 206.1447   0.2648      4234.9570  4234.9570Volume Flow  M3/hr 0.6601     0.0006      12.0614    12.0614Enthalpy  KJ/hr 118158.0000                   --          2.13960E+06                                          1.85927E+06__________________________________________________________________________Stream       16         17          18         19__________________________________________________________________________Name                                INLET LIQUID                                          PLANT INLETVapour frac. 0.9717     0.9526      0.0000     0.9835Temperature  C.    4.2312     -2.8720     5.5843     3.0000   *Pressure  Kpa a 3910.0000  3880.0000   3880.0000  1140.0000                                                   *Molar Flow  Kgmole/hr        200.0000   200.0000    9.0662     547.8779 *Mass Flow  Kg/hr 4234.9570  4234.9570   775.7913   11111.7988Volume Flow  M3/hr 12.0614    12.0614     1.1834     32.1156Enthalpy  KJ/hr 1.65927E+06                   1.54547E+06 -56890.5742                                          4.97228E+06__________________________________________________________________________Stream       20         21          22         23__________________________________________________________________________Name         INLET LIQUID                   1ST SUCTION 1ST DISCHARG                                          RECYCLE GASVapour frac. 0.0000     1.0000      1.0000     1.0000Temperature  C.    3.0000     3.0000      203.3503   50.0000  *Pressure  Kpa a 1140.0000  1140.0000   1155.0000  1140.0000Molar Flow  Kgmole/hr        9.0662     538.8117    71.8124    71.8124Mass Flow  Kg/hr 775.7913   10336.0088  1670.0835  1670.0835Volume Flow  M3/hr 1.1834     30.9322     4.7552     4.7552Enthalpy  KJ/hr -63267.7852                   5.03555E+06 1.45617E+06                                          854163.3750__________________________________________________________________________Stream       24         25          26         27__________________________________________________________________________Name         2ND SUCTION                   2ND DISCHARG           GAS/GAS INVapour frac. 1.0000     1.0000      1.0000     1.0000Temperature  C.    14.1339    111.4896    45.0000  * 45.0000Pressure  Kpa a 1140.0000                 * 3985.0000   3950.0000  3950.0000Molar Flow  Kgmole/hr        663.3459   663.3459    663.3459   463.3459Mass Flow  Kg/hr 14046.2070 14046.2070  14046.2070 9811.2500Volume Flow  M3/hr 40.0043    40.0043     40.0043    27.9430Enthalpy  KJ/hr 6.68286E+06                   9.33890E+06 7.09649E+06                                          4.95688E+06__________________________________________________________________________Stream       28         29          30         31__________________________________________________________________________Name         INLET LIQUID                   LOW TEMP IN LOW TEMP LIQ                                          LOW TEMP LIQVapour frac. 0.9160     0.9056      0.0000     0.2187Temperature  C.    -14.4599   -8.6641     -8.6641    -21.0864Pressure  Kpa a 3880.0000  3880.0000 * 3880.0000  1270.0000Molar Flow  Kgmole/hr        463.3459   672.4121    63.4545    63.4545Mass Flow  Kg/hr 9811.2500  14821.9961  3008.2058  3008.2058Volume Flow  M3/hr 27.9430    41.1877     5.7646     5.7646Enthalpy  KJ/hr 3.12602E+06                   4.61460E+06 -230736.5313                                          -230736.5313__________________________________________________________________________Stream       32         35          37         38__________________________________________________________________________Name         STAB FEED  STAB OVRHEAD                               C5+ PRODUCT                                          C5+ PRODUCTVapour frac. 0.3067     1.0000    * 0.0000     0.0000Temperature  C.    -0.4371    49.0660   * 159.9917 * 37.3449Pressure  Kpa a 1200.0000                 * 1140.0000 * 1150.0000                                        * 1115.0000__________________________________________________________________________ 
    
     
                                           TABLE 22__________________________________________________________________________Processing Natural Gas Containing Asphaltenes (FIG. 4) Exchanger Dutiesand Compressor Power__________________________________________________________________________Stream   71          72          73          74__________________________________________________________________________Name     WARM GAS/GAS                GAS/LIQ     CHILLER     COLD GAS/GASEnthalpyKJ/hr    1.83086E+06 200000.0000                          * 1.24965E+06 765125.0000__________________________________________________________________________Stream   75          76          77          78__________________________________________________________________________Name     SUBCOOLER   DC2 CONDENSE                            COLD REC GAS                                        WARM REC GASEnthalpyKJ/hr    122247.0391 643667.3125                          * 88672.8516  233377.1719__________________________________________________________________________Stream   79          80          81          82__________________________________________________________________________Name     STAB REBOIL 1ST AFTCOOL 2ND AFTCOOL 3RD AFTCOOLEnthalpyKJ/hr    1.11883E+06              * 602006.7500 2.24241E+06 1.68871E+06__________________________________________________________________________Stream   85          86          87          88__________________________________________________________________________Name     LPG EXCHANGE                C5+ COOLER  COLD RES GAS                                        OLD GAS/GASEnthalpyKJ/hr    280327.9063 307832.8750 676452.1250 1.59748E+06__________________________________________________________________________Stream   89          90          91          92__________________________________________________________________________Name     DC2 REBOILER                1ST COMPRESS                            2ND COMPRESS                                        SALES COMPEnthalpyKJ/hr    113806.3672              * 629069.8750 2.65604E+06 1.54860E+ 06Stream   95          96__________________________________________________________________________Name     LPG PUMP    INLET PUMPEnthalpyKJ/hr    5185.0742   6377.2129__________________________________________________________________________ 
    
     
                                           TABLE 23__________________________________________________________________________Processing Natural Gas Containing Asphaltenes Material Balance__________________________________________________________________________Stream         19          37          57          61__________________________________________________________________________Name           PLANT INLET C5+ PRODUCT LPG PRODUCT RESIDUE GASVapour frac.   0.9835      0.0000      0.0001      0.9999Temperature  C.      3.0000    * 159.9917  * -43.8084  * -71.2282  *Pressure  Kpa a   1140.0000 * 1150.0000 * 147.0000  * 3550.0000 *Molar Flow  Kgmole/hr          547.8779  * 10.7296   * 30.5992   * 506.5427  *Mass Flow  Kg/hr   11111.7988  967.9293    1441.8444   8701.7588Volume Flow  M3/hr   32.1156     1.4473      2.8018      27.8659Enthalpy  KJ/hr   4.97228E+06 295021.2188 -274486.0313                                              2.59148E+06Density  Kg/m3   10.6961     514.6133    591.8276    53.8822Mole Wt.       20.2815     90.2109     47.1203     17.1787Spec. Heat  KJ/Kgmole-C.          42.7273     275.3918    98.9779     58.8834Therm Cond  Watt/m-K.          --          --          --          --Viscosity  Cp      --          --          --          --Sur Tension  Dyne/cm --          --          --          --Std Density  Kg/m3   --          --          --          --Z Factor       --          --          --          --N2     Kgmole/hr          9.8725    * 0.0000    * 0.0000    * 9.8725    *CO2    Kgmole/hr          0.1044    * 0.0000    * 0.0002    * 0.1042    *Methane  Kgmole/hr          465.4894  * 0.0000    * 0.0002    * 465.4875  *Ethane Kgmole/hr          33.9973   * 0.0000    * 4.2189    * 29.7761   *Propane  Kgmole/hr          18.1889   * 0.0085    * 16.8796   * 1.3023    *i-Butane  Kgmole/hr          3.9973    * 0.1508    * 3.8459    * 0.0000    *n-Butane  Kgmole/hr          5.3440    * 0.8043    * 4.5367    * 0.0000    *i-Pentan  Kgmole/hr          2.2859    * 1.7006    * 0.5850    * 0.0000    *n-Pentan  Kgmole/hr          2.1665    * 1.7773    * 0.3891    * 0.0000    *n-Hexane  Kgmole/hr          2.1559    * 2.0387    * 0.1171    * 0.0000    *n-Octane  Kgmole/hr          4.2758    * 4.2493    * 0.0265    * 0.0000    *Total  Kgmole/hr          547.8779  * 10.7296   * 30.5992   * 506.5427  *__________________________________________________________________________Stream         30          35          50          54__________________________________________________________________________Name           LOW TEMP LIQ                      STAB OVRHEAD                                  GAS FRAC LIQ                                              DC2 OVERHEADVapour frac.   0.0000      1.0000    * 0.0000      1.0000    *Temperature  C.      -8.6641     49.0660   * -53.1752  * -70.7176  *Pressure  Kpa a   3880.0000   1140.0000 * 3600.0000 * 140.0000  *Molar Flow  Kgmole/hr          63.4545     52.7218   * 102.4116  * 71.8124   *Mass Flow  Kg/hr   3008.2058   2040.1130   3111.9280   1670.0835Volume Flow  M3/hr   5.7646      4.3169      7.5570      4.7552Enthalpy  KJ/hr   -230736.5313                      793143.3750 -404555.0625                                              505050.1250Density  Kg/m3   553.5582    18.7276     477.3377    1.9731Mole Wt.       47.4073     38.6958     30.3865     23.2562Spec. Heat  KJ/Kgmole-C.          111.7226    77.0316     81.8515     39.2520Therm Cond  Watt/m-K.          0.1156      0.0257      0.1182      0.0176Viscosity  Cp      0.1463      0.0104      0.0956      0.0073Sur Tension  Dyne/cm 10.3698     --          7.9553      --Std Density  Kg/m3   519.2969    --          257.7187    --Z Factor       0.1511      0.8792      0.1253      0.9804N2     Kgmole/hr          0.0926      0.0926    * 0.2378    * 0.2378    *CO2    Kgmole/hr          0.0094      0.0094    * 0.0305    * 0.0303    *Methane  Kgmole/hr          14.5182     14.5178   * 42.6154   * 42.6152   *Ethane Kgmole/hr          8.8261      8.8259    * 25.9269   * 21.7080   *Propane  Kgmole/hr          13.8092     13.8010   * 23.5929   * 6.7133    *i-Butane  Kgmole/hr          5.5669      5.4157    * 4.1573    * 0.3114    *n-Butane  Kgmole/hr          9.0181      8.2118    * 4.7257    * 0.1891    *i-Pentan  Kgmole/hr          2.6818      0.9809    * 0.5903    * 0.0053    *n-Pentan  Kgmole/hr          2.4089      0.6315    * 0.3910    * 0.0019    *n-Hexane  Kgmole/hr          2.2192      0.1804    * 0.1172    * 0.0001    *n-Octane  Kgmole/hr          4.3040      0.0547    * 0.0265    * 0.0000    *Total  Kgmole/hr          63.4545     52.7218   * 102.4116  * 71.8124   *__________________________________________________________________________Stream         9__________________________________________________________________________Name           ERRORVapour frac.   --Temperature  C.      --Pressure  Kpa a   --Molar Flow  Kgmole/hr          0.0064Mass Flow  Kg/hr   0.2648Volume Flow  M3/hr   0.0006Enthalpy  KJ/hr   --Density  Kg/m3   --Mole Wt.       41.3224Spec. Heat  KJ/Kgmole-C.          --Therm Cond  Watt/m-K.          --Viscosity  Cp      --Sur Tension  Dyne/cm --Std Density  Kg/m3   --Z Factor       --N2     Kgmole/hr          0.0000CO2    Kgmole/hr          0.0000Methane  Kgmole/hr          0.0017Ethane Kgmole/hr          0.0022Propane  Kgmole/hr          -0.0015i-Butane  Kgmole/hr          0.0006n-Butane  Kgmole/hr          0.0030i-Pentan  Kgmole/hr          0.0002n-Pentan  Kgmole/hr          0.0001n-Hexane  Kgmole/hr          0.0000n-Octane  Kgmole/hr          -0.0000Total  Kgmole/hr          0.0064__________________________________________________________________________ 
    
     
                                           TABLE 24__________________________________________________________________________Processing Natural Gas Containing Asphaltenes (FIG. 4) Stream__________________________________________________________________________CompositionsStream         19          37          56          61__________________________________________________________________________Name           PLANT INLET C5+ PRODUCT DC2 RECYCLE RESIDUE GASVapour frac.   0.9835      0.0000      1.0000      0.9999Temperature  C.      3.0000    * 159.9917  * 35.0000   * -71.2282  *Pressure  Kpa a   1140.0000 * 1150.0000 * 120.0000    3550.0000 *Molar Flow  Kgmole/hr          547.8779  * 10.7296   * 71.8124     506.5427  *Mass Flow  Kg/hr   11111.7988  967.9293    1670.0835   8701.7588Volume Flow  M3/hr   32.1156     1.4473      4.7552      27.8659Enthalpy  KJ/hr   4.97228E+06 295021.2188 827100.1875 2.59148E+06Density  Kg/m3   10.6961     514.6133    1.0949      53.8822Mole Wt.       20.2815     90.2109     23.2562     17.1787Spec. Heat  KJ/Kgmole-C.          42.7273     275.3918    45.9434     58.8834Therm Cond  Watt/m-K.          --          --          0.0301      --Viscosity  Cp      --          --          0.0109      --Sur Tension  Dyne/cm --          --          --          --Std Density  Kg/m3   --          --          --          --Z Factor       --          --          0.9948      --N2             0.0180    * 0.0000    * 0.0033      0.0195    *CO2            0.0002    * 0.0000    * 0.0004      0.0002    *Methane        0.8496    * 0.0000    * 0.5934      0.9190    *Ethane         0.0621    * 0.0000    * 0.3023      0.0588    *Propane        0.0332    * 0.0008    * 0.0935      0.0026    *i-Butane       0.0073    * 0.0141    * 0.0043      0.0000    *n-Butane       0.0098    * 0.0750    * 0.0026      0.0000    *i-Pentan       0.0042    * 0.1585    * 0.0001      0.0000    *n-Pentan       0.0040    * 0.1656    * 0.0000      0.0000    *n-Hexane       0.0039    * 0.1900    * 0.0000      0.0000    *n-Octane       0.0078    * 0.3960    * 0.0000      0.0000    *__________________________________________________________________________Stream         30          35          50          54__________________________________________________________________________Name           LOW TEMP LIQ                      STAB OVRHEAD                                  GAS FRAC LIQ                                              DC2 OVERHEADVapour frac.   0.0000      1.0000    * 0.0000      1.0000    *Temperature  C.      -8.6641     49.0660   * -53.1752  * -70.7176  *Pressure  Kpa a   3880.0000   1140.0000 * 3600.0000 * 140.0000  *Molar Flow  Kgmole/hr          63.4545     52.7218   * 102.4116  * 71.8124   *Mass Flow  Kg/hr   3008.2058   2040.1130   3111.9280   1670.0835Volume Flow  M3/hr   5.7646      4.3169      7.5570      4.7552Enthalpy  KJ/hr   -230736.5313                      793143.3750 -404555.0625                                              505050.1250Density  Kg/m3   553.5582    18.7276     477.3377    1.9731Mole Wt.       47.4073     38.6958     30.3865     23.2562Spec. Heat  KJ/Kgmole-C.          111.7226    77.0316     81.8515     39.2520Therm Cond  Watt/m-K.          0.1156      0.0257      0.1182      0.0176Viscosity  Cp      0.1463      0.0104      0.0956      0.0073Sur Tension  Dyne/cm 10.3698     --          7.9553      --Std Density  Kg/m3   519.2969    --          257.7187    --Z Factor       0.1511      0.8792      0.1253      0.9804N2             0.0015      0.0018    * 0.0023    * 0.0033    *CO2            0.0001      0.0002    * 0.0003    * 0.0004    *Methane        0.2288      0.2754    * 0.4161    * 0.5934    *Ethane         0.1391      0.1674    * 0.2532    * 0.3023    *Propane        0.2176      0.2618    * 0.2304    * 0.0935    *i-Butane       0.0877      0.1027    * 0.0406    * 0.0043    *n-Butane       0.1421      0.1558    * 0.0461    * 0.0026    *i-Pentan       0.0423      0.0186    * 0.0058    * 0.0001    *n-Pentan       0.0380      0.0120    * 0.0038    * 0.0000    *n-Hexane       0.0350      0.0034    * 0.0011    * 0.0000    *n-Octane       0.0678      0.0010    * 0.0003    * 0.0000    *__________________________________________________________________________ 
    
     
                                           TABLE 25__________________________________________________________________________Processing Natural Gas Containing Asphaltenes (FIG. 4) Gas__________________________________________________________________________FractionatorHyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130  Date 1980/1/1  Time 0:5:12*****COMPUTED RESULTS*****    Feed Conditions__________________________________________________________________________   Feed Stream Number              44   Enters on stage              10   Liquid Fraction              0.1350   Temperature              -52.97       C.   Pressure   3600.00      Kpa a   Flowrate   608.96       Kgmole/hr   Enthalpy   2830754.     KJ/hr   N2         10.1103      Kgmole/hr   CO2        0.1347       Kgmole/hr   Methane    508.1042     Kgmole/hr   Ethane     55.7051      Kgmole/hr   Propane    24.8940      Kgmole/hr   i-Butane   4.1575       Kgmole/hr   n-Butane   4.7267       Kgmole/hr   i-Pentan   0.5904       Kgmole/hr   n-Pentan   0.3910       Kgmole/hr   n-Hexane   0.1172       Kgmole/hr   n-Octane   0.0265       Kgmole/hr__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130  Date 1980/1/1  Time 0:5:15***Stage Variables***  Press      Temp    Molar Flow Rates Heat DutyStage  Kpa Deg C.  Liquid                  Vapour   Feed                               GJ/Hour__________________________________________________________________________1      3550.00      -71.228 50.03                  506.54       -0.643672      3585.00      -60.231 35.04                  556.573      3586.88      -56.875 29.46                  541.584      3588.75      -55.550 27.20                  536.015      3590.63      -54.992 26.30                  533.746      3592.50      -54.753 25.85                  532.847      3594.38      -54.619 25.32                  532.398      3596.25      -54.463 24.13                  531.869      3598.13      -54.107 20.92                  530.6810     3600.00      -53.175 102.41                  527.46   608.95__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130  Date 1980/1/1  Time 0:5:43***Products***      Vapour from Stage 1                       Liquid from Stage 10      Kg Mol/Hour              Mol Frc  Kg Mol/Hour                               Mol Frc__________________________________________________________________________N2         9.872   0.01949  0.238   0.00232CO2        0.104   0.00021  0.030   0.00030Methane    465.488 0.91895  42.615  0.41612Ethane     29.776  0.05878  25.927  0.25316Propane    1.302   0.00257  23.593  0.23037i-Butane   0.000   0.00000  4.157   0.04059n-Butane   0.000   0.00000  4.726   0.04614i-Pentan   0.000   0.00000  0.590   0.00576n-Pentan   0.000   0.00000  0.391   0.00382n-Hexane   0.000   0.00000  0.117   0.00114n-Octane   0.000   0.00000  0.026   0.00026Total      506.543          102.412__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130  Date 1980/1/1  Time 0:7:1**PHYSICAL PROPERTIES**VAPOUR LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M ACMH KG/M3  TEMP PRESS__________________________________________________________________________1     17.179 8702.   0.161  53.88098                              1.02670                                   0.766692     17.640 9818.   0.196  50.16525                              1.06250                                   0.773363     17.711 9592.   0.197  48.61880                              1.07759                                   0.774294     17.713 9494.   0.198  47.92205                              1.08494                                   0.775095     17.710 9453.   0.198  47.64312                              1.08818                                   0.775686     17.709 9436.   0.198  47.54356                              1.08958                                   0.776167     17.707 9427.   0.198  47.49774                              1.09039                                   0.776608     17.702 9415.   0.199  47.42375                              1.09144                                   0.777039     17.687 9386.   0.199  47.19811                              1.09393                                   0.7774610    17.642 9306.   0.200  46.53959                              1.10062                                   0.77793__________________________________________________________________________LIQUID LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M3/HR  KG/M3  TEMP PRESS__________________________________________________________________________1     22.312 1116.   2.848  391.93538                              0.84804                                   0.757022     25.412 890.    2.089  426.09707                              0.82216                                   0.768673     26.891 792.    1.794  441.65121                              0.80854                                   0.775204     27.612 751.    1.673  448.98901                              0.80173                                   0.779275     27.924 734.    1.624  452.05298                              0.79889                                   0.781346     28.063 725.    1.599  453.39551                              0.79769                                   0.782527     28.168 713.    1.569  454.43593                              0.79680                                   0.783548     28.357 684.    1.499  456.38768                              0.79510                                   0.785049     28.867 604.    1.308  461.75536                              0.79021                                   0.7882910    30.386 3112.   6.518  477.33949                              0.77555                                   0.79687__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130  Date 1980/1/1  Time 0:8:54**TRANSPORT PROPERTIES**VAPOUR                LIQUID       THERMAL          THERMAL   SURFACESTAGEVISCOSITY       CONDUCTIVITY                 VISCOSITY                        CONDUCTIVITY                                  TENSIONNO.  CP     WATT/M-K  CP     WATT/M-K  DYNE/CM__________________________________________________________________________1    0.00943       0.03002   0.05894                        0.10581   4.45442    0.00968       0.03021   0.07118                        0.11027   5.69303    0.00976       0.03034   0.07771                        0.11256   6.34284    0.00979       0.03042   0.08104                        0.11368   6.66745    0.00980       0.03046   0.08248                        0.11412   6.80386    0.00981       0.03048   0.08311                        0.11431   6.86237    0.00981       0.03049   0.08360                        0.11444   6.90598    0.00981       0.03050   0.08454                        0.11472   6.98909    0.00983       0.03054   0.08720                        0.11557   7.227910   0.00984       0.03061   0.09560                        0.11824   7.9553__________________________________________________________________________ 
    
     
                                           TABLE 26__________________________________________________________________________Processing Natural Gas Containing AsphalteneDepropanizer Column Profiles__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130 Date 1980/1/1 Time 0:22:25*****COMPUTED RESULTS*****    Feed Conditions__________________________________________________________________________   Feed Stream Number              53   Enters on stage              1   Liquid Fraction              0.3220   Temperature              -71.26      C.   Pressure   140.00      Kpa a   Flowrate   102.41      Kgmole/hr   Enthalpy   116865.     KJ/hr   N2         0.2378      Kgmole/hr   CO2        0.0305      Kgmole/hr   Methane    42.6154     Kgmole/hr   Ethane     25.9269     Kgmole/hr   Propane    23.5929     Kgmole/hr   i-Butane   4.1573      Kgmole/hr   n-Butane   4.7257      Kgmole/hr   i-Pentan   0.5903      Kgmole/hr   n-Pentan   0.3910      Kgmole/hr   n-Hexane   0.1172      Kgmole/hr   n-Octane   0.0265      Kgmole/hr__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130 Date 1980/1/1 Time 0:22:28***Stage Variables***  Press      Temp     Molar Flow Rates                               Heat DutyStage  Kpa Deg C.   Liquid                   Vapour  Feed                               GJ/Hour__________________________________________________________________________1      140.00      -70.718  33.08                   71.81   102.412      141.75      -58.110  35.34                   2.483      143.50      -53.726  36.13                   4.744      145.25      -51.267  36.24                   5.535      147.00      -43.808  30.60                   5.64        0.11381__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130  Date 1980/1/1 Time 0:22:37***Products***    Vapour from Stage 1                      Liquid from Stage 5    Kg Mol/Hour            Mol Frc   Kg Mol/Hour                              Mol Frc__________________________________________________________________________N2       0.238   0.00331   0.000   0.00000CO2      0.030   0.00042   0.000   0.00001Methane  42.615  0.59342   0.000   0.00001Ethane   21.708  0.30229   4.219   0.13788Propane  6.713   0.09348   16.880  0.55163i-Butane 0.311   0.00434   3.846   0.12568n-Butane 0.189   0.00263   4.537   0.14826i-Pentan 0.005   0.00007   0.585   0.01912n-Pentan 0.002   0.00003   0.389   0.01272n-Hexane 0.000   0.00000   0.117   0.00383n-Octane 0.000   0.00000   0.026   0.00087Total    71.812            30.599__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130 Date 1980/1/1 Time 0:23:50**PHYSICAL PROPERTIES**VAPOUR LEAVING FROM EACH STAGE        FLOW          DENSITY                             REDUCEDSTAGE MOL WT KG/HOUR M ACMH                      KG/M3  TEMP PRESS__________________________________________________________________________1     23.256 1670.   0.846 1.97309                             0.83115                                  0.029992     30.224  75.    0.030 2.46594                             0.72685                                  0.030113     33.231 157.    0.058 2.70232                             0.68994                                  0.030414     34.124 189.    0.068 2.78075                             0.68606                                  0.030895     36.207 204.    0.071 2.89192                             0.68899                                  0.03187__________________________________________________________________________LIQUID LEAVING FROM EACH STAGE        FLOW          DENSITY                             REDUCED STAGE MOL WT KG/HOUR M3/HR KG/M3  TEMP PRESS__________________________________________________________________________1     45.855 1517.   2.437 622.37499                             0.54479                                  0.033302     45.258 1599.   2.638 606.23793                             0.58165                                  0.033453     45.132 1630.   2.713 600.83349                             0.59400                                  0.033804     45.422 1646.   2.746 599.40916                             0.59850                                  0.034315     47.120 1442.   2.408 598.79915                             0.60719                                  0.03531__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130 Date 1980/1/1 Time 0:25:2**TRANSPORT PROPERTIES**VAPOUR                LIQUID       THERMAL          THERMAL   SURFACESTAGEVISCOSITY       CONDUCTIVITY                 VISCOSITY                        CONDUCTIVITY                                  TENSIONNO.  CP     WATT/M-K  CP     WATT/M-K  DYNE/CM__________________________________________________________________________1    0.00731       0.01760   0.30619                        0.15775   19.57942    0.00698       0.01483   0.25408                        0.14797   17.68913    0.00679       0.01397   0.23864                        0.14468   17.06264    0.00678       0.01390   0.23428                        0.14298   16.83615    0.00687       0.01406   0.22867                        0.13822   16.4071__________________________________________________________________________ 
    
     
                                           TABLE 27__________________________________________________________________________Processing Natural Gas Containing Asphaltenes (FIG. 4)Stabilizer Column Profiles__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130 Date 1980/1/1 Time 0:30:29*****COMPUTED RESULTS*****    Feed Conditions__________________________________________________________________________   Feed Stream Number              32   Enters on stage              1   Liquid Fraction              0.6933   Temperature              -0.44       C.   Pressure   1200.00     Kpa a   Flowrate   63.45       Kgmole/hr   Enthalpy   -30737.     KJ/hr   N2         0.0926      Kgmole/hr   CO2        0.0094      Kgmole/hr   Methane    14.5182     Kgmole/hr   Ethane     8.8261      Kgmole/hr   Propane    13.8092     Kgmole/hr   i-Butane   5.5669      Kgmole/hr   n-Butane   9.0181      Kgmole/hr   i-Pentan   2.6818      Kgmole/hr   n-Pentan   2.4089      Kgmole/hr   n-Hexane   2.2192      Kgmole/hr   n-Octane   4.3040      Kgmole/hr__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130 Date 1980/1/1 Time 0:30:32***Stage Variables***  Press      Temp     Molar Flow Rates                               Heat DutyStage  Kpa Deg C.   Liquid                   Vapour  Feed                               GJ/Hour__________________________________________________________________________1      1140.00      49.066   51.91                   52.72   63.452      1141.67      82.863   60.85                   41.183      1143.33      95.566   62.35                   50.124      1145.00      105.433  61.88                   51.625      1146.67      116.247  59.41                   51.156      1148.33      132.003  53.52                   48.687      1150.00      159.992  10.73                   42.79       1.11884__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130 Date 1980/1/1 Time 0:30:47***Products***    Vapour from Stage 1                      Liquid from Stage 7    Kg Mol/Hour            Mol Frc   Kg Mol/Hour                              Mol Frc__________________________________________________________________________N2       0.093   0.00176   0.000   0.00000CO2      0.009   0.00018   0.000   0.00000Methane  14.518  0.27537   0.000   0.00000Ethane   8.826   0.16741   0.000   0.00000Propane  13.801  0.26177   0.008   0.00079i-Butane 5.416   0.10272   0.151   0.01406n-Butane 8.212   0.15576   0.804   0.07496i-Pentan 0.981   0.01861   1.701   0.15850n-Pentan 0.632   0.01198   1.777   0.16564n-Hexane 0.180   0.00342   2.039   0.19001n-Octane 0.055   0.00104   4.249   0.39604Total    52.722            10.730__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130 Date 1980/1/1 Time 0:32:0**PHYSICAL PROPERTIES**VAPOUR LEAVING FROM EACH STAGE        FLOW          DENSITY                             REDUCEDSTAGE MOL WT KG/HOUR M ACMH                      KG/M3  TEMP PRESS__________________________________________________________________________1     38.696 2040.   0.109 18.72761                             0.99017                                  0.265212     54.113 2228.   0.087 25.61780                             0.88592                                  0.292673     58.987 2956.   0.107 27.52899                             0.87517                                  0.305074     62.115 3206.   0.113 28.49352                             0.87563                                  0.313405     65.193 3334.   0.114 29.24127                             0.88002                                  0.321496     69.155 3367.   0.113 29.85412                             0.89116                                  0.331637     76.311 3266.   0.106 30.81944                             0.91272                                  0.34914__________________________________________________________________________LIQUID LEAVING FROM EACH STAGE        FLOW          DENSITY                             REDUCEDSTAGE MOL WT KG/HOUR M3/HR KG/M3  TEMP PRESS__________________________________________________________________________1     61.575 3196.   5.783 552.63897                             0.75943                                  0.307042     64.493 3924.   7.549 519.75557                             0.81465                                  0.315863     66.950 4174.   8.135 513.06397                             0.82713                                  0.323024     69.532 4302.   8.419 510.98426                             0.83342                                  0.330265     72.957 4335.   8.482 510.97845                             0.83796                                  0.339496     79.097 4233.   8.235 514.00144                             0.84103                                  0.355177     90.211  968.   1.880 514.82869                             0.84871                                  0.38442__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name AESGKM.130 Date 1980/1/1 Time 0:33:31**TRANSPORT PROPERTIES**VAPOUR                LIQUID       THERMAL          THERMAL   SURFACESTAGEVISCOSITY       CONDUCTIVITY                 VISCOSITY                        CONDUCTIVITY                                  TENSIONNO.  CP     WATT/M-K  CP     WATT/M-K  DYNE/CM__________________________________________________________________________1    0.01037       0.02566   0.14420                        0.09890   9.34162    0.00989       0.02561   0.11526                        0.08830   6.76953    0.00988       0.02622   0.11029                        0.08592   6.20304    0.00993       0.02683   0.10880                        0.08482   5.92645    0.01003       0.02754   0.10968                        0.08414   5.74056    0.01020       0.02865   0.10969                        0.08377   5.64677    0.01047       0.03060   0.11426                        0.08270   5.3594__________________________________________________________________________ 
    
     
                                           TABLE 28__________________________________________________________________________CO2 RECOVERY FROM NATURAL GAS (FIG. 5)Stream Properties__________________________________________________________________________Stream         1           2           3           4__________________________________________________________________________Name           PLANT INLET COOL INLET  CHILLED INLE                                              COLD INLETVapour frac.   1.0000      0.7384      0.1917      0.1655Temperature   C.     25.0000   * -16.6747    -33.4921    -36.5218Pressure   Kpa a  2800.0000 * 2775.0000   2750.0000   2725.0000Molar Flow   Kgmole/hr          10385.4014                    * 10385.4014  10385.4014  10385.4014Mass Flow   Kg/hr  417768.5625 417768.5625 417768.5625 417768.5625Volume Flow   M3/hr  550.8240    550.8240    550.8240    550.8240Enthalpy   KJ/hr  8.63445E+07 3.49572E+07 -4.08999E+07                                              -4.61006E+07__________________________________________________________________________Stream         5           6           7           10__________________________________________________________________________Name           COLD INLET  COLD INLET  TOWER 2 IN  TOWER 2 LIQVapour frac.   0.0891      0.0887      0.0794      0.0000Temperature   C.     -50.0000  * -50.5795    -53.6560    -53.8331  *Pressure   Kpa a  2700.0000   2675.0000   2650.0000   2650.0000 *Molar Flow   Kgmole/hr          10385.4014  10385.4014  10385.4014  11144.7090                                                        *Mass Flow   Kg/hr  417768.5625 417768.5625 417768.5625 462993.0000Volume Flow   M3/hr  550.8240    550.8240    550.8240    593.7190Enthalpy   KJ/hr  -6.41006E+07                      -6.46275E+07                                  -6.78210E+07                                              -8.47391E+07__________________________________________________________________________Stream         11          12          13          16__________________________________________________________________________Name           TOWER 2 LIQ TOWER 2 LIQ TOWER 3 IN  TOWER 1 LIQVapour frac.   0.0370      0.1020      0.1748      0.0000    *Temperature   C.     -56.0000  * -42.7272    -53.0000  * -53.1730  *Pressure   Kpa a  1995.1183   1945.1183   1078.5044   4510.0000 *Molar Flow   Kgmole/hr          11144.7090  11144.7090  11144.7090  775.6005  *Mass Flow   Kg/hr  462993.0000 462993.0000 462993.0000 24162.2441Volume Flow   M3/hr  593.7190    593.7190    593.7190    45.2904Enthalpy   KJ/hr  -8.47391E+07                      -6.67391E+07                                  -6.67391E+07                                              -2.02202E+06__________________________________________________________________________Stream         17          18          19          20__________________________________________________________________________Name           TOWER 1 LIQ TOWER 1 LIQ TOWER 2 IN  RICH RECYCLEVapour frac.   0.2127      0.2777      0.2777      1.0000Temperature   C.     -65.5695    -61.8000  * -61.8000    -53.0117  *Pressure   Kpa a  2690.0000   2640.0000 * 2640.0000 * 1078.0000 *Molar Flow   Kgmole/hr          775.6005    775.6005    775.6005    2084.3000 *Mass Flow   Kg/hr  24162.2441  24162.2441  24162.2441  68293.9531Volume Flow   M3/hr  45.2904     45.2904     45.2904     110.3548Enthalpy   KJ/hr  -2.02202E+06                      -1.49516E+06                                  -1.49516E+06                                              1.32186E+07__________________________________________________________________________Stream         21          22          23          24__________________________________________________________________________Name           RICH RECYCLE                      RICH RECYCLE                                  RICH RECYCLE                                              RICH RECYCLEVapour frac.   1.0000      1.0000      1.0000      1.0000Temperature   C.     -40.0000  * 30.0000   * 113.9608    40.0000   *Pressure   Kpa a  1063.0000   1048.0000   2600.0000 * 2575.0000Molar Flow   Kgmole/hr          2084.3000   2084.3000   2084.3000   2084.3000Mass Flow   Kg/hr  68293.9531  68293.9531  68293.9531  68293.9531Volume Flow   M3/hr  110.3548    110.3548    110.3548    110.3548Enthalpy   KJ/hr  1.42573E+07 1.97926E+07 2.61530E+07 1.97039E+07__________________________________________________________________________Stream         25          26          27          28__________________________________________________________________________Name           RICH RECYCLE                      RICH RECYCLE                                  RICH RECYCLE                                              RICH RECYCLEVapour frac.   1.0000      1.0000      1.0000      0.2175Temperature   C.     136.6700    40.0000   * -1.3821     -37.0000  *Pressure   Kap a  7000.0000 * 6975.0000   6950.0000   6915.0000Molar Flow   Kgmole/hr          12084.3000  2084.3000   84.3000     2084.3000Mass Flow   Kg/hr  68293.9531  68293.9531  68293.9531  68293.9531Volume Flow   M3/hr  110.3548    110.3548    110.3548    110.3548Enthalpy   KJ/hr  2.66999E+07 1.68751E+07 1.13398E+07 -2.31788E+06__________________________________________________________________________Stream         29          30__________________________________________________________________________Name           RICH RECYCLE                      RICH RECYCLEVapour frac.   0.1557      0.4483Temperature   C.     -40.9340    -59.5289Pressure   Kpa a  6890.0000   2645.0000 *Molar Flow   Kgmole/hr          2084.3000   2084.3000Mass Flow   Kg/hr  68293.9531  68293.9531Volume Flow   M3/hr  110.3548    110.3548Enthalpy   KJ/hr  -3.35664E+06                      -3.35664E+06__________________________________________________________________________Stream         31          32          33          34__________________________________________________________________________Name           TOWER 1 OVHD                      TOWER 1 OVHD                                  TOWER 1 OVHD                                              TOWER 1 OVHDVapour frac.   1.0000      1.0000      1.0000      1.0000Temperature   C.     -86.5613  * -40.0000  * 30.0000   * 118.0826Pressure   Kpa a  4500.0000 * 4475.0000   4450.0000   11030.0000                                                        *Molar Flow   Kgmole/hr          4739.1123 * 4739.1123   4739.1123   4739.1123Mass Flow   Kg/hr  82398.6641  82398.6641  82398.6641  82398.6641Volume Flow   M3/hr  245.0641    245.0641    245.0641    245.0641Enthalpy   KJ/hr  1.66680E+07 3.04782E+07 4.42419E+07 5.83821E+07__________________________________________________________________________Stream         36          37          38          39__________________________________________________________________________Name           TOWER 1 OVHD                      TOWER 1 OVHD                                  TOWER 1 OVHD                                              TOWER 1 OVHDVapour frac.   1.0000      1.0000      1.0000      1.0000Temperature   C.     40.0000   * -17.5416    -37.0000  * -71.3393Pressure   Kpa a  10990.0000  10950.0000  10910.0000  10870.0000Molar Flow   Kgmole/hr          4739.1123   4739.1123   4739.1123   4739.1123Mass Flow   Kg/hr  82398.6641  82398.6641  82398.6641  82398.6641Volume Flow   M3/hr  245.0641    245.0641    245.0641    245.0641Enthalpy   KJ/hr  4.17958E+07 2.80321E+07 2.21869E+07 8.37669E+06__________________________________________________________________________Stream         40__________________________________________________________________________Name           TOWER 1 OVHDVapour frac.   0.2790Temperature   C.     -88.5402Pressure   Kpa a  4705.0000Molar Flow   Kgmole/hr          4739.1123Mass Flow   Kg/hr  82398.6641Volume Flow   M3/hr  245.0641Enthalpy   KJ/hr  8.37669E+06__________________________________________________________________________Stream         41          42          43          44__________________________________________________________________________Name           RESIDUE GAS RESIDUE GAS RESIDUE GAS RESIDUE GASVapour frac.   1.0000      1.0000      1.0000      1.0000Temperature   C.     -88.5402    -54.0000  * 20.0000   * 58.5390Pressure   Kpa a  4705.0000   4665.0000   4625.0000 * 7021.0000 *Molar Flow   Kgmole/hr          1322.2645   1322.2645   1322.2645   1322.2645Mass Flow   Kg/hr  23006.9531  23006.9531  23006.9531  23006.9531Volume Flow   M3/hr  67.3341     67.3341     67.3341     67.3341Enthalpy   KJ/hr  4.42822E+06 7.62175E+06 1.17624E+07 1.33924E+07__________________________________________________________________________Stream         45          50          51          52__________________________________________________________________________Name           RESIDUE GAS REFLUX      REFLUX      LEAN RECYCLEVapour frac.   1.0000      0.0000      0.0927      1.0000    *Temperature   C.     50.0000   * -88.5402    -89.7443    -62.4926  *Pressure   Kpa a  6986.0000   4705.0000   4500.0000 * 2640.0000 *Molar Flow   Kgmole/hr          1322.2645   3416.8477   3416.8477   2099.6677 *Mass Flow   Kg/hr  23006.9531  59391.7109  59391.7109  47190.8320Volume Flow   M3/hr  67.3341     177.7300    177.7300    112.7118Enthalpy   KJ/hr  1.29289E+07 3.94846E+06 3.94846E+06 1.20528E+07__________________________________________________________________________Stream         53          54          55          56__________________________________________________________________________Name           LEAN RECYCLE                      LEAN RECYCLE                                  LEAN RECYCLE                                              LEAN RECYCLEVapour frac.   1.0000      1.0000      1.0000      1.0000Temperature   C.     -40.0000  * 30.0000   * 83.3703     40.0000   *Pressure   Kpa a  2615.0000   2590.0000   4650.0000   4615.0000Molar Flow   Kgmole/hr          2099.6677   2099.6677   2099.6677   2099.6677Mass Flow   Kg/hr  47190.8320  47190.8320  47190.8320  47190.8320Volume Flow   M3/hr  112.7118    112.7118    112.7118    112.7118Enthalpy   KJ/hr  1.41230E+07 2.00661E+07 2.39540E+07 2.00677E+07__________________________________________________________________________Stream         57          58          59          60__________________________________________________________________________Name           LEAN RECYCLE                      LEAN RECYCLE                                  LEAN RECYCLE                                              CO2 PRODUCTVapour frac.   1.0000      1.0000      0.9863      0.0000Temperature   C.     -23.8615    -37.0000  * -53.0428    -47.5295  *Pressure   Kpa a  4580.0000   4545.0000   4510.0000 * 1091.0000 *Molar Flow   Kgmole/hr          2099.6677   2099.6677   2099.6677   9061.1396 *Mass Flow   Kg/hr  47190.8320  47190.8320  47190.8320  394722.2188Volume Flow   M3/hr  112.7118    112.7118    112.7118    483.4119Enthalpy   KJ/hr  1.41246E+07 1.27740E+07 1.07038E+07 -7.47548E+07__________________________________________________________________________Stream         61          62__________________________________________________________________________Name           CO2 PRODUCT CO2 PRODUCTVapour frac.   0.0000      1.0000Temperature   C.     -38.2464    20.0000   *Pressure   Kpa a  14601.0000  14566.0000                                *Molar Flow   Kgmole/hr          9061.1396   9061.1396Mass Flow   Kg/hr  394722.2188 394722.2188Volume Flow   M3/hr  483.4119    483.4119Enthalpy   KJ/hr  -6.72514E+07                      -2.00047E+07__________________________________________________________________________ 
    
     
                                           TABLE 29__________________________________________________________________________CO2 Recovery from Natural Gas (FIG. 5)Exchanger Duties and Compressor power__________________________________________________________________________Stream   70        71        72          73__________________________________________________________________________Name     WARM GAS/GAS              FEED CHILLER                        DC1 REBOILER                                    GAS/LIQ #2EnthalpyKJ/hr    5.13873E+07              7.58572E+07                        5.20067E+06                                  * 1.80000E+07                                              *__________________________________________________________________________Stream   74        75        76          77__________________________________________________________________________Name     GAS/LIQ #3              COLD GAS/GAS                        GAS/LIQ #1  RICH CHILLEREnthalpyKJ/hr    526864.1250              3.19353E+06                        4.72466E+07 1.36577E+07__________________________________________________________________________Stream   78        79        80          81__________________________________________________________________________Name     LEAN CHILLER              OVHD CHILLER                        1ST AFTCOOL 2ND AFTCOOLEnthalpyKJ/hr    1.35063E+06              5.84519E+06                        6.44905E+06 9.82480E+06__________________________________________________________________________Stream   82        83        84          85__________________________________________________________________________Name     3RD AFTCOOL              4TH AFTCOOL                        5TH AFTCOOL WARM RES GASEnthalpyKJ/hr    3.88634E+06              1.65863E+07                        463526.0000 4.14065E+06__________________________________________________________________________Stream   90        91        92          93__________________________________________________________________________Name     1ST COMPRESS              2ND COMPRESS                        3RD COMPRESS                                    4TH COMPRESSEnthalpyKJ/hr    6.36039E+06              6.99597E+06                        3.88797E+06 1.41402E+07__________________________________________________________________________Stream   94        95__________________________________________________________________________Name     5TH COMPRESS              CO2 PUMPEnthalpyKJ/hr    1.63004E+06              7.50339E+ 06__________________________________________________________________________ 
    
     
                                           TABLE 30__________________________________________________________________________CO2 Recovery from Natural Gas (FIG. 5)Material Balance__________________________________________________________________________Stream          1           41          60         9__________________________________________________________________________Name            PLANT INLET RESIDUE GAS CO2 PRODUCTVapour frac.    1.0000      1.0000      0.0000     --Temperature   C.      25.0000   * -88.5402    -47.5295 * --Pressure   Kpa a   2800.0000 * 4705.0000   1091.0000                                            * --Molar Flow   Kgmole/hr           10385.4014                     * 1322.2645   9061.1396                                            * 1.9971Mass Flow   Kg/hr   417768.5625 23006.9531  394722.2188                                              39.3932Volume Flow   M3/hr   550.8240    67.3341     483.4119   0.0780Enthalpy   KJ/hr   8.63445E+07 4.42822E+06 -7.47548E+07                                              --Density Kg/m3   53.0194     116.1075    1121.6316  --Mole Wt.        40.2265     17.3997     43.5621    19.7255Spec. Heat   KJ/Kgmole-C           44.9537     176.2348    81.8874    --Therm Cond   Watt/m-K           0.0245      0.0374      0.1710     --Viscosity   Cp      0.0155      0.0117      0.1891     --Sur Tension   Dyne/cm --          --          16.4346    --Std Density   Kg/m3   --          --          801.2128   --Z Factor        0.8570      0.4594      0.0226     --Hydrogen   Kgmole/hr           26.8140   * 26.7866     0.0000   * 0.0274N2      Kgmole/hr           147.4790  * 145.5366    1.6354   * 0.3070H2S     Kgmole/hr           0.1160    * 0.0000      0.1160   * 0.0000CO2     Kgmole/hr           8906.0234 * 14.8683     8890.6504                                            * 0.5046Methane Kgmole/hr           1266.9810 * 1134.2388   130.8671 * 1.8751Ethane  Kgmole/hr           26.8140   * 0.8344      26.7005  * -0.7208Propane Kgmole/hr           11.1730   * 0.0000      11.1702  * 0.0028Total   Kgmole/hr           10385.4014                     * 1322.2645   9061.1396                                            * 1.9971__________________________________________________________________________Stream          51          19          13         30__________________________________________________________________________Name            REFLUX      TOWER 2 IN  TOWER 3 IN RICH RECYCLEVapour frac.    0.0927      0.2777      0.1748     0.4483Temperature   C.      -89.7443    -61.8000    -53.0000 * -59.5289Pressure   Kpa a   4500.0000 * 2640.0000 * 1078.5044  2645.0000 *Molar Flow   Kgmole/hr           3416.8477   775.6005    11144.7090 2084.3000Mass Flow   Kg/hr   59391.7109  24162.2441  462993.0000                                              68293.9531Volume Flow   M3/hr   177.7300    45.2904     593.7190   110.3548Enthalpy   KJ/hr   3.94846E+06 -1.49516E+06                                   -6.67391E+07                                              -3.35664E+06Density Kg/m3   232.3282    177.5339    139.6074   124.8427Mole Wt.        17.3820     31.1530     41.5438    32.7659Spec. Heat   KJ/Kgmole-C           185.7925    70.4770     72.4842    62.4287Therm Cond   Watt/m-K           --          --          --         --Viscosity   Cp      --          --          --         --Sur Tension   Dyne/cm --          --          --         --Std Density   Kg/m3   --          --          --         --Z Factor        --          --          --         --Hydrogen   Kgmole/hr           25.1014     0.7734      3.9149     3.9153N2      Kgmole/hr           240.8509    13.5097     68.4562    66.8309H2S     Kgmole/hr           0.0000      0.0020      0.1298     0.0138CO2     Kgmole/hr           70.2442     345.7680    10100.0986 1209.7102Methane Kgmole/hr           3074.9607   280.3562    916.4879   785.7894Ethane  Kgmole/hr           5.6904      135.0509    42.6535    16.2424Propane Kgmole/hr           0.0000      0.1403      12.9678    1.7981Total   Kgmole/hr           3416.8477   775.6005    11144.7090 2084.3000__________________________________________________________________________Stream          59          40__________________________________________________________________________Name            LEAN RECYCLE                       TOWER 1 OVHDVapour frac.    0.9863      0.2790Temperature   C.      -53.0428    -88.5402Pressure   Kpa a   4510.0000 * 4705.0000Molar Flow   Kgmole/hr           2099.6677   4739.1123Mass Flow   Kg/hr   47190.8320  82398.6641Volume Flow   M3/hr   112.7118    245.0641Enthalpy   KJ/hr   1.07038E+07 8.37669E+06Density Kg/m3   85.1440     188.1072Mole Wt.        22.4754     17.3869Spec. Heat   KJ/Kgmole-C           64.1362     207.5904Therm Cond   Watt/m-K           --          --Viscosity   Cp      --          --Sur Tension   Dyne/cm --          --Std Density   Kg/m3   --          --Z Factor        --          --Hydrogen   Kgmole/hr           27.5910     51.8880N2      Kgmole/hr           159.3602    386.3875H2S     Kgmole/hr           0.0020      0.0000CO2     Kgmole/hr           360.2976    85.1125Methane Kgmole/hr           1416.4723   4209.1997Ethane  Kgmole/hr           135.8043    6.5247Propane Kgmole/hr           0.1403      0.0000Total   Kgmole/hr           2099.6677   4739.1123__________________________________________________________________________ 
    
     
                                           TABLE 31__________________________________________________________________________CO2 Recovery from Natural Gas (FIG. 5)Stream Compositions__________________________________________________________________________Stream          41          60__________________________________________________________________________Name            DEHY OUTLET LPG REID VPVapour frac.    1.0000      0.0000    *Temperature   C.      -8.7406     37.7778   *Pressure   Kpa a   3870.0000 * 1397.7695Molar Flow   Kgmole/hr           608.9576    30.5992Mass Flow   Kg/hr   11813.7881  1441.8444Volume Flow   M3/hr   35.4232     2.8018Enthalpy   KJ/hr   4.84553E+06 11026.9502Density Kg/m3   41.5299     491.6014Mole Wt.        19.4000     47.1203Spec. Heat   KJ/Kgmole-C           48.1491     134.8213Therm Cond   Watt/m-K           --          0.0923Viscosity   Cp      --          0.0955Sur Tension   Dyne/cm --          6.2805Std Density   Kg/m3   --          525.6946Z Factor        --          0.0518N2              0.0166      0.0000CO2             0.0002      0.0000Methane         0.8344      0.0000Ethane          0.0915      0.1379Propane         0.0409      0.5516i-Butane        0.0068      0.1257n-Butane        0.0078      0.1483i-Pentan        0.0010      0.0191n-Pentan        0.0006      0.0127n-Hexane        0.0002      0.0038n-Octane        0.0000      0.0009__________________________________________________________________________Stream          51          19          30         59__________________________________________________________________________Name            GAS FRAC LIQ                       PLANT INLET LOW TEMP LIQ                                              LPG PRODUCTVapour frac.    0.0000      0.9835      0.0000     0.0000Temperature   C.      -68.2282    3.0000    * -8.6641    37.7988Pressure   Kpa a   3550.0000   1140.0000 * 3880.0000  1470.0000 *Molar Flow   Kgmole/hr           102.4116    547.8779  * 63.4545    30.5992Mass Flow   Kg/hr   3111.9280   11111.7988  3008.2058  1441.8444Volume Flow   M3/hr   7.5570      32.1156     5.7646     2.8018Enthalpy   KJ/hr   -526802.1250                       4.97228E+06 -230736.5313                                              11026.9502Density Kg/m3   502.0868    10.6961     553.5582   491.5682Mole Wt.        30.3865     20.2815     47.4073    47.1203Spec. Heat   KJ/Kgmole-C           76.8780     42.7273     111.7226   134.6348Therm Cond   Watt/m-K           0.1322      --          0.1156     0.0923Viscosity   Cp      0.1167      --          0.1463     0.0954Sur Tension   Dyne/cm 10.1259     --          10.3698    6.2781Std Density   Kg/m3   257.7187    --          519.2969   525.6946Z Factor        0.1261      --          0.1511     0.0545N2              0.0023      0.0180    * 0.0015     0.0000CO2             0.0003      0.0002    * 0.0001     0.0000Methane         0.4161      0.8496    * 0.2288     0.0000Ethane          0.2532      0.0621    * 0.1391     0.1379Propane         0.2304      0.0332    * 0.2176     0.5516i-Butane        0.0406      0.0073    * 0.0877     0.1257n-Butane        0.0461      0.0098    * 0.1421     0.1483i-Pentan        0.0058      0.0042    * 0.0423     0.0191n-Pentan        0.0038      0.0040    * 0.0380     0.0127n-Hexane        0.0011      0.0039    * 0.0350     0.0038n-Octane        0.0003      0.0078    * 0.0678     0.0009__________________________________________________________________________Stream          40__________________________________________________________________________Name            LOW TEMP GASVapour frac.    1.0000Temperature   C.      -8.6641Pressure   Kpa a   3880.0000Molar Flow   Kgmole/hr           608.9576Mass Flow   Kg/hr   11813.7881Volume Flow   M3/hr   35.4232Enthalpy   KJ/hr   4.84553E+06Density Kg/m3   41.6423Mole Wt.   19.4000Spec. Heat   KJ/Kgmole-C           48.1800Therm Cond   Watt/m-K           0.0336Viscosity   Cp      0.0112Sur Tension   Dyne/cm --Std Density   Kg/m3   --Z Factor        0.8220N2              0.0166CO2             0.0002Methane         0.8344Ethane          0.0915Propane         0.0409i-Butane        0.0068n-Butane        0.0078i-Pentan        0.0010n-Pentan        0.0006n-Hexane        0.0002n-Octane        0.0000__________________________________________________________________________Stream          1           41          60__________________________________________________________________________Name            PLANT INLET RESIDUE GAS CO2 PRODUCTVapour frac.    1.0000      1.0000      0.0000Temperature   C.      25.0000   * -88.5402    -47.5295 *Pressure   Kpa a   2800.0000 * 4705.0000   1091.0000                                            *Molar Flow   Kgmole/hr           10385.4014                     * 1322.2645   9061.1396                                            *Mass Flow   Kg/hr   417768.5625 23006.9531  394722.2188Volume Flow   M3/hr   550.8240    67.3341     483.4119Enthalpy   KJ/hr   8.63445E+07 4.42822E+06 -7.47548E+07Density Kg/m3   53.0194     116.1075    1121.6316Mole Wt.        40.2265__________________________________________________________________________Stream          1           41          60__________________________________________________________________________Name            PLANT INLET RESIDUE GAS CO2 PRODUCTVapour frac.    1.0000      1.0000      0.0000Temperature   C.      25.0000   * -88.5402    -47.5295 *Pressure   Kpa a   2800.0000 * 4705.0000   1091.0000                                            *Molar Flow   Kgmole/hr           10385.4014                     * 1322.2645   9061.1396                                            *Mass Flow   Kg/hr   417768.5625 23006.9531  394722.2188Volume Flow   M3/hr   550.8240    67.3341     483.4119Enthalpy   KJ/hr   8.63445E+07 4.42822E+06 -7.47548E+07Density Kg/m3   53.0194     116.1075    1121.6316Mole Wt.        40.2265     17.3997     43.5621Spec. Heat   KJ/Kgmole-C           44.9537     176.2348    81.8874Therm Cond   Watt/m-K           0.0245      0.0374      0.1710Viscosity   Cp      0.0155      0.0117      0.1891Sur Tension   Dyne/cm --          --          16.4346Std Density   Kg/m3   --          --          801.2128Z Factor        0.8570      0.4594      0.0226Hydrogen        0.0026    * 0.0203      0.0000   *N2              0.0142    * 0.1101      0.0002   *H2S             0.0000    * 0.0000      0.0000   *CO2             0.8576    * 0.0112      0.9812   *Methane         0.1220    * 0.8578      0.0144   *Ethane          0.0026    * 0.0006      0.0029   *Propane         0.0011    * 0.0000      0.0012   *__________________________________________________________________________Stream          51          19          13         30__________________________________________________________________________Name            REFLUX      TOWER 2 IN  TOWER 3 IN RICH RECYCLEVapour frac.    0.0927      0.2777      0.1748     0.4483Temperature   C.      -89.7443    -61.8000    -53.0000 * -59.5289Pressure   Kpa a   4500.0000 * 2640.0000 * 1078.5044  2645.0000 *Molar Flow   Kgmole/hr           3416.8477   775.6005    11144.7090 2084.3000Mass Flow   Kg/hr   59391.7109  24162.2441  462993.0000                                              68293.9531Volume Flow   M3/hr   177.7300    45.2904     593.7190   110.3548Enthalpy   KJ/hr   3.94846E+06 -1.49516E+06                                   -6.67391E+07                                              -3.35664E+06Density Kg/m3   232.3282    177.5339    139.6074   124.8427Mole Wt.        17.3820     31.1530     41.5438    32.7659Spec. Heat   KJ/Kgmole-C           185.7925    70.4770     72.4842    62.4287Therm Cond   Watt/m-K           --          --          --         --Viscosity   Cp      --          --          --         --Sur Tension   Dyne/cm --          --          --         --Std Density   Kg/m3   --          --          --         --Z Factor        --          --          --         --Hydrogen        0.0073      0.0010      0.0004     0.0019N2              0.0705      0.0174      0.0061     0.0321H2S             0.0000      0.0000      0.0000     0.0000CO2             0.0206      0.4458      0.9063     0.5804Methane         0.8999      0.3615      0.0822     0.3770Ethane          0.0017      0.1741      0.0038     0.0078Propane         0.0000      0.0002      0.0012     0.0009__________________________________________________________________________Stream          59          40__________________________________________________________________________Name            LEAN RECYCLE                       TOWER 1 OVHDVapour frac.    0.9863      0.2790Temperature   C.      -53.0428    -88.5402Pressure   Kpa a   4510.0000 * 4705.0000Molar Flow   Kgmole/hr           2099.6677   4739.1123Mass Flow   Kg/hr   47190.8320  82398.6641Volume Flow   M3/hr   112.7118    245.0641Enthalpy   KJ/hr   1.07038E+07 8.37669E+06Density Kg/m3   85.1440     188.1072Mole Wt.        22.4754     17.3869Spec. Heat   KJ/Kgmole-C           64.1362     207.5904Therm Cond   Watt/m-K           --          --Viscosity   Cp      --          --Sur Tension   Dyne/cm --          --Std Density   Kg/m3   --          --Z Factor        --          --Hydrogen        0.0131      0.0109N2              0.0759      0.0815H2S             0.0000      0.0000CO2             0.1716      0.0180Methane         0.6746      0.8882Ethane          0.0647      0.0014Propane         0.0001      0.0000__________________________________________________________________________ 
    
     
                                           TABLE 32__________________________________________________________________________CO2 Recovery from Natural GasCO2 Freezing Points__________________________________________________________________________C          Stream      7 CO2 freezing point is                                  -59.879__________________________________________________________________________Stream     12 CO2 freezing point is                  -59.024 CStream     13 CO2 freezing point is                  -57.482 CStream     30 CO2 freezing point is                  -60.622 CStream     59 CO2 freezing point is                  -72.463 CStream     40 CO2 freezing point is                  -114.484 CStream     50 CO2 freezing point is                  -112.407 CStream     51 CO2 freezing point is                  -112.354 CStream     18 CO2 freezing point is                  -66.940 CStream     19 CO2 freezing point is                  -66.940 C__________________________________________________________________________Stream  7           12        13        30__________________________________________________________________________Name    TOWER 2 IN  TOWER 2 LIQ                         TOWER 3 IN                                   RICH RECYCLETemperature C   -53.6560    -42.7272  -53.0000                                 * -59.5289__________________________________________________________________________Stream  59          40        50        51__________________________________________________________________________Name    LEAN RECYCLE               TOWER 1 OVHD                         REFLUX    REFLUXTemperature C   -53.0428    -88.5402  -88.5402  -89.7443__________________________________________________________________________Stream  18          19__________________________________________________________________________Name    TOWER 1 LIQ TOWER 2 INTemperature C   -61.8000  * -61.8000__________________________________________________________________________ 
    
     
                                           TABLE 33__________________________________________________________________________CO2 Recovery from Natural Gas (FIG. 5)Tower 1 Column Profiles__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/ 1/ 1  Time 6:10:33COMPUTED RESULTS   Feed Conditions   Feed Stream Number 51__________________________________________________________________________   Enters on stage    1   Liquid Fraction    0.9073   Temperature        -89.74                           C   Pressure           4500.00                           Kpa a   Flowrate           3416.85                           Kgmole/hr   Enthalpy           3948466.                           KJ/hr   Hydrogen           25.1014                           Kgmole/hr   N2                 240.8509                           Kgmole/hr   H2S                0.0000                           Kgmole/hr   CO2                70.2442                           Kgmole/hr   Methane            3074.9607                           Kgmole/hr   Ethane             5.6904                           Kgmole/hr   Propane            0.0000                           Kgmole/hr__________________________________________________________________________   Feed Stream Number 59__________________________________________________________________________   Enters on stage    10   Liquid Fraction    0.0137   Temperature        -53.04                           C   Pressure           4510.00                           Kpa a   Flowrate           2099.67                           Kgmole/hr   Enthalpy           10703807.                           KJ/hr   Hydrogen           27.5910                           Kgmole/hr   N2                 159.3602                           Kgmole/hr   H2S                0.0020                           Kgmole/hr   CO2                360.2976                           Kgmole/hr   Methane            1416.4723                           Kgmole/hr   Ethane             135.8043                           Kgmole/hr   Propane            0.1403                           Kgmole/hr__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/ 1/ 1  Time 6:10:37Stage Variables   Press       Temp   Molar Flow Rates Heat DutyStage   Kpa Deg C  Liquid                   Vapour  Feed                               GJ/Hour__________________________________________________________________________1       4500.00       -86.561              2997.02                   4739.11 3415.052       4501.11       -84.211              2584.55                   4321.093       4502.22       -81.606              2015.62                   3908.614       4503.33       -77.485              1436.01                   3339.695       4504.44       -70.652              1018.66                   2760.076       4505.56       -62.483              832.37                   2342.727       4506.67       -56.934              774.53                   2156.448       4507.78       -54.451              757.18                   2098.609       4508.89       -53.514              750.74                   2081.2510      4510.00       -53.173              775.60                   2074.80 2099.67__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/ 1/ 1  Time 6:11:24Products      Vapour from Stage 1                        Liquid from Stage 10      Kg Mol/Hour              Mol Frc   Kg Mol/Hour                               Mol Frc__________________________________________________________________________Hydrogen   51.888  0.01095   0.773  0.00100N2         386.387 0.08153   13.510 0.01742H2S        0.000   0.00000   0.002  0.00000CO2        85.112  0.01796   345.768                               0.44581Methane    4209.200              0.88818   280.356                               0.36147Ethane     6.525   0.00138   135.051                               0.17412Propane    0.000   0.00000   0.140  0.00018Total      4739.112          775.600__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/ 1/ 1  Time 6:12:21PHYSICAL PROPERTIESVAPOUR LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M ACMH KG/M3  TEMP PRESS__________________________________________________________________________1     17.387 82399.  0.770  106.98844                              1.00315                                   0.987242     17.536 75776.  0.723  104.83648                              1.00204                                   0.976533     17.881 69889.  0.695  100.59366                              1.00448                                   0.967874     18.478 61712.  0.653  94.56502                              1.01197                                   0.957955     19.428 53622.  0.609  88.07607                              1.02618                                   0.944526     20.650 48377.  0.574  84.34648                              1.03996                                   0.927997     21.601 46580.  0.557  83.55990                              1.04573                                   0.915158     22.064 46303.  0.554  83.59234                              1.04719                                   0.908889     22.247 46302.  0.553  83.67741                              1.04756                                   0.9064610    22.319 46308.  0.553  83.73256                              1.04770                                   0.90555__________________________________________________________________________LIQUID LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M3/HR  KG/M3  TEMP PRESS__________________________________________________________________________1     17.600 52748.  197.470                       267.08103                              0.97433                                   0.964022     18.131 46861.  165.756                       282.67140                              0.96789                                   0.949333     19.192 38684.  122.737                       315.13469                              0.95346                                   0.928594     21.305 30595.  81.088 377.24825                              0.92474                                   0.893775     24.884 25348.  53.297 475.54196                              0.88245                                   0.842476     28.295 23552.  42.026 560.33710                              0.85521                                   0.799427     30.050 23275.  38.847 599.05380                              0.84814                                   0.779128     30.737 23273.  37.950 613.17751                              0.84688                                   0.771489     31.008 23279.  37.600 619.02878                              0.84645                                   0.7684310    31.153 24162.  38.788 622.84466                              0.84595                                   0.76666__________________________________________________________________________ Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/ 1/ 1  Time 6:14:17TRANSPORT PROPERTIESVAPOUR                LIQUID       THERMAL          THERMAL   SURFACESTAGEVISCOSITY       CONDUCTIVITY                 VISCOSITY                        CONDUCTIVITY                                  TENSIONNO.  CP     WATT/M-K  CP     WATT/M-K  DYNE/CM__________________________________________________________________________1    0.01128       0.03602   0.02582                        0.06917   0.34452    0.01123       0.03574   0.02758                        0.07197   0.46363    0.01110       0.03500   0.03139                        0.07746   0.77384    0.01096       0.03395   0.03938                        0.08737   1.55835    0.01094       0.03287   0.05403                        0.10153   3.15586    0.01111       0.03212   0.06828                        0.11141   4.63647    0.01131       0.03174   0.07487                        0.11455   5.22118    0.01141       0.03158   0.07714                        0.11534   5.39509    0.01145       0.03152   0.07803                        0.11566   5.461710   0.01147       0.03150   0.07859                        0.11596   5.5101__________________________________________________________________________ 
    
     
                                           TABLE 34__________________________________________________________________________CO2 Recovery from Natural Gas (FIG. 5)Tower #2 Column Profiles__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/ 1/ 1  Time 6:26:32Stage Variables  Press      Temp    Molar Flow Rates  Heat DutyStage  Kpa Deg C   Liquid                   Vapour  Feed GJ/Hour__________________________________________________________________________1      2640.00      -62.493  510.55                   2099.67  774.672      2641.43      -61.315  452.85                   1835.543      2642.86      -59.590 1587.38                   1777.85  2084.304      2644.29      -58.438 1581.67                   828.075      2645.71      -57.117 1585.10                   822.366      2647.14      -55.969 1586.76                   825.807      2648.57      -54.931 1584.01                   827.458      2650.00      -53.833 11144.71                   824.70  10385.40__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/ 1/ 1  Tlme 6:25:56COMPUTED RESULTS   Feed Conditions   Feed Stream Number                     19__________________________________________________________________________   Enters on stage   1   Liquid Fraction   0.7223   Temperature       -61.80                           C   Pressure          2640.00                           Kpa a   Flowrate          775.60                           Kgmole/hr   Enthalpy          -1495162.                           KJ/hr   Hydrogen          0.7734                           Kgmole/hr   N2                13.5097                           Kgmole/hr   H2S               0.0020                           Kgmole/hr   CO2               345.7680                           Kgmole/hr   Methane           280.3562                           Kgmole/hr   Ethane            135.0509                           Kgmole/hr   Propane           0.1403                           Kgmole/hr__________________________________________________________________________   Feed Stream Number                     30__________________________________________________________________________   Enters on stage   3   Liquid Fraction   0.5517   Temperature       -59.53                           C   Pressure          2645.00                           Kpa a   Flowrate          2084.30                           Kgmole/hr   Enthalpy          -3356640.                           KJ/hr   Hydrogen          3.9153                           Kgmole/hr   N2                66.8309                           Kgmole/hr   H2S               0.0138                           Kgmole/hr   CO2               1209.7102                           Kgmole/hr   Methane           785.7894                           Kgmole/hr   Ethane            16.2424                           Kgmole/hr   Propane           1.7981                           Kgmole/hr__________________________________________________________________________   Feed Stream Number                     7__________________________________________________________________________   Enters on stage   8   Liquid Fraction   0.9206   Temperature       -53.66                           C   Pressure          2650.00                           Kpa a   Flowrate          10385.40                           Kgmole/hr   Enthalpy          -67821064.                           KJ/hr   Hydrogen          26.8140                           Kgmole/hr   N2                147.4790                           Kgmole/hr   H2S               0.1160                           Kgmole/hr   CO2               8906.0234                           Kgmole/hr   Methane           1266.9810                           Kgmole/hr   Ethane            26.8140                           Kgmole/hr   Propane           11.1730                           Kgmole/hr__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/ 1/ 1  Time 6:27:17Products      Vapour from Stage 1                        Liquid from Stage 8      Kg Mol/Hour              Mol Frc   Kg Mol/Hour                               Mol Frc__________________________________________________________________________Hydrogen   27.591  0.01314   3.915  0.00035N2         159.360 0.07590   68.456 0.00614H2S        0.002   0.00000   0.130  0.00001CO2        360.298 0.17160   10100.099                               0.90627Methane    1416.472              0.67462   916.488                               0.08224Ethane     135.804 0.06468   42.654 0.00383Propane    0.140   0.00007   12.968 0.00116Total      2099.668          11144.709__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/ 1/ 1  Time 6:28:12PHYSICAL PROPERTIESVAPOUR LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M ACMH KG/M3  TEMP PRESS__________________________________________________________________________1     22.475 47191.  1.092  43.21873                              0.99954                                   0.528372     22.737 41734.  0.972  42.94365                              1.00983                                   0.525033     22.987 40867.  0.962  42.49892                              1.02168                                   0.520384     23.363 19346.  0.455  42.48059                              1.03754                                   0.524255     23.725 19510.  0.456  42.80409                              1.03849                                   0.521686     24.012 19829.  0.461  43.05540                              1.03840                                   0.518887     24.258 20072.  0.464  43.22425                              1.03926                                   0.516218     24.495 20201.  0.467  43.29175                              1.04220                                   0.51325__________________________________________________________________________LIQUID LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M3/HR  KG/M3  TEMP PRESS__________________________________________________________________________1     36.561 18666.  21.948  850.33990                              0.74706                                   0.408512     39.301 17798.  18.257  974.67885                              0.73491                                   0.386643     40.677 64570.  62.108 1039.50602                              0.73322                                   0.376434     40.928 64735.  61.907 1045.54310                              0.73498                                   0.375495     41.041 65053.  62.199 1045.74618                              0.73849                                   0.375086     41.151 65297.  62.360 1046.94054                              0.74154                                   0.374597     41.304 65425.  62.235 1051.11949                              0.74411                                   0.373728     41.544 462993. 436.600                       1060.30578                              0.74658                                   0.37213__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/ 1/ 1  Time 6:40:12TRANSPORT PROPERTIESVAPOUR                LIQUID       THERMAL          THERMAL   SURFACESTAGEVISCOSITY       CONDUCTIVITY                 VISCOSITY                        CONDUCTIVITY                                  TENSIONNO.  CP     WATT/M-K  CP     WATT/M-K  DYNE/CM__________________________________________________________________________1    0.00979       0.02615   0.14385                        0.15613   12.54392    0.00992       0.02630   0.17041                        0.16791   14.73173    0.01006       0.02650   0.18300                        0.17244   15.66914    0.01025       0.02684   0.18366                        0.17197   15.65715    0.01035       0.02680   0.18198                        0.17070   15.45776    0.01043       0.02677   0.18067                        0.16970   15.29607    0.01050       0.02676   0.18010                        0.16904   15.19768    0.01059       0.02681   0.18039                        0.16872   15.1639__________________________________________________________________________ 
    
     
                                           TABLE 35__________________________________________________________________________CO.sub.2 Recovery from Natural Gas (FIG. 5) Tower #3 Column__________________________________________________________________________ProfilesHyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/1/1  Time 6:48:38COMPUTED RESULTS   Feed Conditions   Feed Stream Number              13   Enters on stage              1   Liquid Fraction              0.8252   Temperature              -53.00       C.   Pressure   1078.50      Kpa a   Flowrate   11144.71     Kgmole/hr   Enthalpy   -66739136.   KJ/hr   Hydrogen   3.9149       Kgmole/hr   N2         68.4562      Kgmole/hr   H2S        0.1298       Kgmole/hr   CO2        10100.0986   Kgmole/hr   Methane    916.4879     Kgmole/hr   Ethane     42.6535      Kgmole/hr   Propane    12.9678      Kgmole/hr__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/1/1  Time 6:48:40Stage Variables  Press      Temp    Molar Flow Rates Heat DutyStage  Kpa Deg C.  Liquid                  Vapour   Feed                               GJ/Hour__________________________________________________________________________1      1078.00      -53.012 9196.32                  2084.30  11145.442      1079.44      -52.985 9198.54                  135.183      1080.89      -52.967 9200.10                  137.404      1082.33      -52.951 9201.65                  138.965      1083.78      -52.931 9203.45                  140.516      1085.22      -52.904 9205.71                  142.317      1086.67      -52.854 9208.95                  144.578      1088.11      -52.699 9216.26                  147.819      1089.56      -51.863 9248.90                  155.1210     1091.00      -47.529 9061.14                  187.76       5.20068__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/1/1  Time 6:48:55Products      Vapour from Stage 1                       Liquid from Stage 10      Kg Mol/Hour              Mol Frc  Kg Mol/Hour                               Mol Frc__________________________________________________________________________Hydrogen     3.915 0.00188    0.000 0.00000N2          66.831 0.03206    1.635 0.00018H2S          0.014 0.00001    0.116 0.00001CO2        1209.710              0.58039  8890.650                               0.98118Methane     785.789              0.37700   130.867                               0.01444Ethane      16.242 0.00779   26.700 0.00295Propane      1.798 0.00086   11.170 0.00123Total      2084.300         9061.140__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/1/1  Time 6:49:53PHYSICAL PROPERTIESVAPOUR LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M ACMH KG/M3  TEMP PRESS__________________________________________________________________________1     32.766 68294.  3.173  21.52612                              0.86235                                   0.174132     32.784 4432.   0.205  21.57129                              0.86185                                   0.174273     32.778 4504.   0.209  21.59811                              0.86182                                   0.174494     32.763 4553.   0.211  21.61886                              0.86185                                   0.174725     32.744 4601.   0.213  21.63665                              0.86180                                   0.174946     32.721 4657.   0.215  21.65238                              0.86159                                   0.175137     32.702 4728.   0.218  21.66941                              0.86109                                   0.175248     32.734 4839.   0.223  21.71471                              0.85983                                   0.175139     33.180 5147.   0.234  21.98564                              0.85494                                   0.1737710    36.008 6761.   0.287  23.58070                              0.83165                                   0.16612__________________________________________________________________________LIQUID LEAVING FROM EACH STAGE        FLOW           DENSITY                              REDUCEDSTAGE MOL WT KG/HOUR M3/HR  KG/M3  TEMP PRESS__________________________________________________________________________1     43.404 399154. 351.733                       1134.66520                              0.72913                                   0.147302     43.401 399226. 351.863                       1134.45226                              0.72924                                   0.147513     43.399 399275. 351.951                       1134.30609                              0.72932                                   0.147714     43.397 399323. 352.038                       1134.16244                              0.72939                                   0.147915     43.394 399379. 352.139                       1133.99545                              0.72947                                   0.148116     43.392 399450. 352.268                       1133.78310                              0.72958                                   0.148317     43.388 399561. 352.459                       1133.48374                              0.72976                                   0.148518     43.387 399869. 352.912                       1132.90289                              0.73027                                   0.148719     43.409 401483. 354.986                       1130.82985                              0.73279                                   0.1488610    43.562 394722. 351.868                       1121.63561                              0.74557                                   0.14874__________________________________________________________________________Hyprotech&#39;s Process Simulator HYSIM - Licensed to Bob StothersCase Name SHELL610  Date 1980/1/1  Time 6:51:49TRANSPORT PROPERTIESVAPOUR                LIQUID       THERMAL          THERMAL   SURFACESTAGEVISCOSITY       CONDUCTIVITY                 VISCOSITY                        CONDUCTIVITY                                  TENSIONNO.  CP     WATT/M-K  CP     WATT/M-K  DYNE/CM__________________________________________________________________________1    0.01034       0.01892   0.20880                        0.17764   17.64352    0.01034       0.01888   0.20868                        0.17759   17.63263    0.01033       0.01888   0.20859                        0.17756   17.62534    0.01033       0.01889   0.20852                        0.17753   17.61845    0.01033       0.01890   0.20046                        0.17749   17.61056    0.01032       0.01891   0.20034                        0.17745   17.60047    0.01031       0.01893   0.20017                        0.17737   17.58478    0.01031       0.01892   0.19975                        0.17716   17.54499    0.01035       0.01876   0.19789                        0.17614   17.357910   0.01074       0.01772   0.18914                        0.17104   16.4346__________________________________________________________________________