Abstract:
An improved process for separating a hydrocarbon bearing feed gas containing methane and lighter, C 2  (ethylene and/or ethane), and heavier components into a fraction containing predominantly methane and lighter components and a fraction containing predominantly C 2  and heavier hydrocarbon components including the steps of cooling and partially condensing and delivering the feed stream to a separator to provide a first residue vapor and a first liquid containing C 2 , directing a first part of the first liquid containing C 2  into a heavy-ends fractionation column wherein the liquid is separated into a second hydrocarbon bearing vapor residue and a second liquid product containing C 2 ; further cooling the second part of the first liquid containing C 2  and partially condensing the second hydrocarbon bearing vapor residue; combining the cooled second part of the first liquid and partially condensed second hydrocarbon-bearing vapor residue and directing them to a second separator effecting a third residue and a third liquid; cooling and directing a first part of the third liquid into the lights-ends fractionation column, to thereby condense C 2 &#39;s and heavier components while the methane is evaporated in the light-ends fractionation column to thereby obtain fourth residue vapor and liquid, heating and supplying the fourth liquid recovered from the light-ends fractionation column to the heavy-ends fractionation column as a feed thereto; conducting the second part of the third liquid to the heavy-ends fractionation column as a feed thereto.

Description:
BACKGROUND OF THE INVENTION  
         [0001]    1. Field of the Invention  
           [0002]    This invention relates to an improved process for separating a hydrocarbon-bearing feed gas which contains methane and lighter components, (not necessarily all hydrocarbon components), C 2  (ethylene and ethane), and heavier hydrocarbon components into two fractions. The first fraction contains predominantly methane and lighter components and the second fraction contains the recovered desirable C 2  and heavier components. More particularly, this invention relates to a process and apparatus wherein the yield of C 2           s is increased or alternatively energy consumption is reduced for a given C 2  recovery.  
           [0003]    2. The Prior Art  
           [0004]    Hydrocarbon-bearing gas may contain lighter components (e.g., hydrogen, nitrogen, etc.) methane, ethane, and/or ethylene, and a substantial quantity of hydrocarbons of higher molecular weight, for example, propane, butane, pentane and often their unsaturated analogs. Recent changes in ethylene/ethane demand have created increased markets for ethylene/ethane and have created a need for more efficient processes which yield higher recovery levels of this product. In more recent times, the use of cryogenic processes utilizing the principle of gas expansion through a mechanical device to produce power while simultaneously extracting heat from the system have been employed. The use of such equipment depends upon the pressure of the gas source, the composition of the gas and the desired end results. In the typical cryogenic expansion-type recovery processes used in the prior art, a gas stream under pressure is cooled by heat exchange with other streams of the process and/or external sources of cooling are employed such as refrigeration systems. As the gas is cooled, liquids are condensed and are collected and separated so as to thereby obtain desired hydrocarbons. The high pressure liquid feed is typically transferred to a demethanizer column after the pressure is adjusted to the operating pressure of the demethanizer. In column after the pressure is adjusted to the operating pressure of the demethanizer. In such fractionating column the liquid feed is fractionated to separate the residual methane and lighter components from the desired products of ethylene/ethane and heavier hydrocarbon components. In the ideal operation of such separation processes, the vapors leaving the process contain substantially all of the methane and lighter components found in the feed gas and substantially no ethylene/ethane or heavier hydrocarbon components remain. The bottom fraction leaving the demethanizer typically contains substantially all of the ethylene/ethane and heavier hydrocarbon components with very little methane or lighter components which is discharged in the fluid gas outlet from the demethanizer.  
           [0005]    A patentability search was conducted on the present invention and the following references were uncovered.  
                                                       Inventor   U.S. Pat. No.   Issue Date                           Harandi   4,664,784   5/12/1987           Buck et al   4,895,584   1/23/1990           Campbell et al   5,771,712   9/01/1998           Wilkinson et al   5,699,507   6/30/1998                      
 
           [0006]    U.S. Pat. No. 4,664,784—Issued May 12, 1987  
           [0007]    M. N. Harandi to Mobil Oil Corporation  
           [0008]    In a reference directed to fractionation of hydrocarbon mixtures, teachings are found on column 4, line 32 et sequitur re: a zone (81) wherein a descending liquid heavy-ends portion contacts an ascending vaporous light-ends portion so as “ . . . to aid in heat transfer between vapor and liquid.” (column 4, line 44).  
           [0009]    U.S. Pat. No. 4,895,584—Issued Jan. 23, 1990  
           [0010]    L. L. Buck et al to Pro-Quip Corporation  
           [0011]    A reference that claims an improved process for hydrocarbon separation and teaches supplying of the liquids recovered from the light-ends fractionating column to the heavy ends fractionating column and directing part of the (C 2  containing) liquid from a first step into intimate contact with a second residue, which liquid provides additional liquefied methane which acts with the partially condensed second residue as a direct contact refrigerant to thereby condense C 2  and heavier comprising hydrocarbons while methane itself is evaporated in the light-ends fractionation column.  
           [0012]    On column 1, lines 56-67 the following teachings are found: “ . . . feed gas is first cooled and partially condensed and delivered to a separator to provide a first residue vapor and a liquid containing C 2  . . . Part of the liquid containing C 2  from the separator may be directed into a heavy-ends fractionation column wherein the liquid is separated into a second residue containing lighter hydrocarbons and C 2  containing products. A part of the first residue vapors with at least part of the partially condensed second residue are counter currently contacted and commingled in a light-ends fractionation column (emphasis added) . . . ” 
           [0013]    On column 2, lines 1-10 the following teachings are found: “The liquids recovered from the light-ends fractionation column are then fed to the heavy-ends fractionation column as a liquid feed. A portion of the liquids containing C 2  from the separator is fed into intimate contact with the second residue prior to discharging the commingled liquids and gases into the light-ends fractionation column to thereby achieve mass and heat transfer (emphasis added) to thereby liquefy a higher percent of the C 2  and heavier hydrocarbon components while the methane is vaporized” (column 2, lines 1-10).  
           [0014]    The following Elcor Corporation references describe the recovery of C 3  and heavier hydrocarbons via processes wherein counter-current contact of a stream drawn from a deethanizer with a stream in a separator/absorber takes place:  
           [0015]    U.S. Pat. No. 5,799,507—Issued Sep. 1, 1998  
           [0016]    J. D. Wilkinson et al to Elcor Corporation  
           [0017]    See column 4, line 2 re: “ . . . liquid portion of expanded stream commingles with liquids falling downward from the absorbing section . . . ” I.o.w., the stream (36) from the deethanizer (17) flows through heat exchanger (20) to become Stream (36 a ) which flows into the upper section of separator (15) where it “ . . . contacts the vapors rising upward through the absorption section” (column 5, lines 3-4).  
           [0018]    U.S. Pat. No. 5,771,712—Issued Jun. 30, 1998  
           [0019]    R. E. Campbell et al to Elcor Corporation  
           [0020]    This reference teaches essentially the same as Wilkinson et al.  
           [0021]    None of the foregoing patents discussed above embody the present invention.  
         SUMMARY OF THE INVENTION  
         [0022]    The present invention provides processes for increasing the ethylene and ethane component of the discharge from the process unit at reduced energy consumption than the prior art. The foregoing advantage is achieved in the present invention by a process in which the feed gas is first cooled and partially condensed and delivered to a separator to provide a first residue vapor and a first liquid containing C 2  which liquid also contains lighter hydrocarbons. A first part of the first liquid containing C 2  from the separator may be directed into a heavy-ends fractionation column, wherein the liquid is separated into a second residue containing lighter hydrocarbons and a second liquid product containing C 2 . A second part of the first liquid from the separator is cooled. The second residue is cooled and partially condensed and then combined with the cooled second part of the first liquid providing, upon separation, a third residue and a third liquid. A first part of the third liquid is cooled and fed to the light-ends fractionation column. A second part of the third liquid is fed directly to the heavy-ends fractionation column. A part of the first residue vapor with a cooled first part of the third liquid are counter-currently contacted and commingled in a light-ends fractionation column to thereby provide fourth residue vapor and liquid which are separately discharged. Cooling the first part of the third liquid prior to its introduction into the light-ends fractionation column aids in mass and heat transfer. This cooling thereby provides for greater liquefaction of a higher percent of the C 2  and heavier hydrocarbon components while the methane contained in the first part of the third liquid is vaporized. The fourth liquid recovered from the light-ends fractionation column is heated then introduced to the heavy-ends fractionation column as a feed.  
           [0023]    A better understanding of the invention will be had with reference to the following description and claims, taken in conjunction with the attached drawings. 
       
    
    
     DESCRIPTION OF THE DRAWINGS  
       [0024]    [0024]FIG. 1 is a schematic flow diagram illustrating a method of practicing a preferred embodiment of the invention.  
         [0025]    [0025]FIG. 2 is a schematic flow diagram illustrating a variation in the preferred embodiment of the present invention. 
     
    
     DESCRIPTION OF THE PREFERRED EMBODIMENTS  
       [0026]    The improved processes of the present disclosure include the steps of cooling a gaseous hydrocarbon-containing feed stream to form a first vapor stream and a first liquid stream. A first part of the first liquid stream is transferred to a heavy-ends fractionation column while the first vapor stream is transferred to the bottom of a light-ends fractionation column. The heavy-ends fractionation column overhead vapor, which consists mainly of methane, ethylene, and/or ethane, is cooled and partially condensed. The cooled heavy-ends fractionation column overhead is combined with a cooled second part of the first liquid stream. The resulting stream is fed to a separator and separated into a third residue vapor and a third liquid. A first part of the third liquid is cooled and fed to the upper portion of the light-ends fractionation column. The liquid flows downwardly within the light-ends fractionation column and contacts gaseous ethylene and/or ethane and heavier hydrocarbons that flow upwardly. The methane portion of the liquid stream is vaporized by absorbing heat from the gaseous ethylene/ethane and heavier hydrocarbons which causes the ethylene/ethane and heavier hydrocarbons to condense and exit at the bottom of the light-ends fractionation column. The gaseous methane and lighter components within the light-ends fractionation column are removed from the overhead as a product of the process. The second part of the third liquid may be used to reflux the heavy-ends fractionation column. The fourth liquid at the bottom of the light-ends fractionation column is removed and used to cool other process streams; the thus-heated fourth liquid is fed to the upper portion of the heavy-ends fractionation column. The liquid at the bottom of the heavy-ends fractionation column is removed as a product of the process.  
         [0027]    The improved process of this invention is illustrated in a first embodiment in FIG. 1. The incoming gas stream  1  at a temperature of 120° F. and a pressure of 827 psia passes through heat exchanger  38 , so that the temperature thereof is reduced to about −72° F. with attendant partial condensation. Pressure is reduced as the gas flows through the heat exchangers resulting in a pressure of 812 psia at −72° F. at which the raw gas is delivered into a separator  44 . Within separator  44  the cooled gas stream is separated into a first liquid stream (stream  4 ) and a first residue vapor, stream  3 . Stream  3  is passed through a turbo expander  46 . The shaft of turbo expander  46  is connected directly to the shaft of the booster compressor  32 . From the turbo expander, the first residue gas having a temperature of about −163° F. at 200 psia passes by way of stream  5  into a light-ends fractionation column  52 .  
         [0028]    From separator  44  a first part of the first liquid containing C 2  is conducted into a heavy-ends fractionation column  56  by way of stream  4 A. A second part of the first liquid containing C 2  from stream  4  is channeled by way of stream  4 B through heat exchanger  42  where its temperature is decreased. The cooled liquid exits the heat exchanger and combines with the cooled residue stream  14  to form stream  16 .  
         [0029]    The second residue from heavy-ends fractionation column  56 , having a temperature of about −132° F., is fed by way of stream  14  through heat exchanger  42 , combines with the remainder of the liquid containing C 2  from stream  4 B above, and by way of stream  16  into the reflux separator  57 . A first part of the third liquid from the reflux separator  57  is routed by stream  23  through heat exchanger  42  where its temperature is reduced. This liquid stream is then passed as stream  23 A into the light-ends fractionation column  52 . The liquid from stream  23 A passes downwardly through the light-ends fractionation column  52  and encounters the rising first residue gas from stream  5  so that mass and latent heat transfer occur. The second part of the third liquid from the reflux separator  57  is routed by stream  26  to the heavy-ends fractionation column  56 .  
         [0030]    The light-ends fractionation column  52  functions as a combination heat and mass transfer device. The column has two feed streams; that is, streams  5  and  23 A, and two product streams; that is, streams  10  and  9 . The light-ends fractionation column  52  consists of at least one, and preferably more, theoretical liquid-vapor equilibrium stages.  
         [0031]    Vapor enters the light-ends fractionation column by way of stream  5  as a bottom feed while the top feed is by way of stream  23 A which is a liquid enriched by condensed methane. The methane and lighter constituents and un-recovered ethylene and ethane, exit as a dew point vapor as a fourth residue (stream  9 ) from the top tray or separation stage of the light-ends fractionation column  52 .  
         [0032]    The top feed through stream  23 A into the light-ends fractionation column  52  and particularly the methane content thereof serves as a reflux in the column. In flowing from stage to stage within column  52 , the liquid methane is vaporized and in turn the liquid is progressively enriched in ethylene and ethane condensed from the upflowing bottom feed vapor from stream  5 .  
         [0033]    The fourth liquid stream from the light-ends fractionation column  52 , stream  10 , provides process cooling in exchanger  42  while it is itself warmed and then fed to the heavy-ends fractionation column  56  for further separation.  
         [0034]    The fourth residue gas (stream  9 ) discharged from light-ends fractionation column  52  passes through exchangers  42  and  38  and exits the heat exchanger system as stream  19 . The third residue gas vapor in stream  18  exiting the reflux separator  57  also pass through exchangers  42  and  38  and exit the heat exchanger system as stream  28 . The warmed vapor from the light-ends fractionation column (stream  19 ) is compressed in compressor  48  to the same pressure as stream  28  and combined with stream  28  to form stream  30 . The combined vapors of stream  30  are compressed in the booster compressor  32 . At this stage, the methane rich off-gas in stream  21  has a temperature of 103° F. and a pressure of 187 psia. If it is desired to return the discharge gas to the same system from which the raw gas was taken, such as for further transportation of the gas, the pressure will need to be raised back to that substantially equal to the incoming pressure of 827 psia in stream  1 .  
         [0035]    The second liquid discharge, rich in C 2  content, from the lower end of the heavy-ends fractionation column  56  is passed by way of stream  15  and exchanger  38  to product discharge stream  22 .  
         [0036]    The result of a simulation of the process of FIG. 1 is set forth in Table 1A wherein the moles per hour of various constituents of the streams are set forth. The process achieves a recovery of about 97.37 percent of the C 2  content of the feed gas in addition to substantially complete recovery of the C 3  and heavier hydrocarbon components of the feed gas stream into the less volatile fraction (product).  
         [0037]    Table 1B relates the moles per hour of various constituents of the stream of the process of FIG. 1 when the process of FIG. 1 is applied to a feed gas stream that is enriched in ethane and heavier components.  
         [0038]    [0038]FIG. 2 shows an alternate embodiment of the invention. The components of the process of FIG. 2 having the same basic structure and function of those of the system of FIG. 1 are given like numbers. The process is as described with reference to FIG. 1, except that the booster compressor  32  is placed on the feed gas (stream  1 ) and streams  9  and  18  are combined prior to exchanger  42 .  
         [0039]    Table 2, shows the result of a simulation of the system of FIG. 2. Table 2 provides the moles per hour of various constituents for the various streams of this embodiment of the process. The process achieves a recovery of about 91.64 percent of the ethylene and 96.77 percent of the ethane content of the feed gas in addition to substantially complete recovery of the C 3  and heavier hydrocarbon components of the feed gas stream in to the less volatile fraction (product).  
         [0040]    The process has been illustrated using various standard components employed for the sequence of treating steps with it being understood that the process may be practiced utilizing different physical apparatus. For instance, the turbo expander can, in many instances, be eliminated or replaced by a Joule-Thomson isenthalpic control valve. The difference is that where the expander is eliminated or where the Joule-Thomson valve is substituted for the turbo expander, normally greater inlet and refrigeration compression duties are required.  
         [0041]    A different arrangement has been shown in the alternate embodiment for cooling the second residue effluent and thus providing reflux to the light-ends fractionation and heavy-ends fractionation columns.  
         [0042]    Some of the processes in each instance may use multiple turbo expanders. The desirability of the use of multiple turbo expanders is predicated primarily upon the amount of hydrogen content of the inlet gas in stream  1 . It is understood that, according to the inlet gas content, only single turbo expanders may be employed in practicing the process; or, in some instances as previously indicated, turbo expanders may be eliminated completely or substituted by one or more Joule-Thomson isenthalpic expansion valves.  
         [0043]    An important feature of the process is the employment of the light-ends fractionation column  52  which functions as a combination heat and mass transfer device. The use of the reflux in the top stage means that the liquid methane of the reflux is vaporized; and in turn the liquid is progressively enriched in ethylene and ethane condensed from the upflowing bottom feed vapor to thereby recover a higher percent of the C 2  components.  
         [0044]    While the invention has been described with a certain degree of particularity, it is manifest that many changes may be made in the details of construction and the arrangement of components without departing from the spirit and scope of this disclosure. It is understood that the invention is not limited to the embodiments set forth herein for purposes of exemplification, but is to be limited only by the scope of the attached claim or claims, including the full range of equivalency to which each element thereof is entitled.  
                                                                                                                           TABLE 1A                       THE PRO-QUIP CORPORATION                                STREAM   STREAM NUMBER            NAME   1   3   4   5   9   10   14   16   18   23               NITROGEN   9917   9386   531   9386   9274   250   781   781   6.43   1.38       CARBON   8.64   619   245   619   189   583   195   195   0.42   1.53       DIOXIDE       METHANE   7552.91   6526.79   1026 12   6526 79   6374 89   1115 68   2131 34   2131 34   1168 58   963 78       ETHANE   486 41   272 65   213 76   272 65   9 22   299 03   39 18   39 18   3 57   35 60       PROPANE   198 31   56.60   141 71   56 60   0 04   58 45   1 92   1 92   0 03   1 89       I-BUTANE   36.66   5 59   31.07   5.59   0 00   5.67   0 08   0 08   0 00   0.08       N-BUTANE   63 30   7.19   56 11   7 19   0 00   7 27   0 08   0 08   0 00   0.08       I-PENTANE   20 83   1.16   19 67   1 16   0.00   1 17   0 01   0 01   0 00   0.01       N-PENTANE   20.63   0.86   19 77   0 86   0.00   0 86   0 00   0 00   0 00   0 00       HEXANE   19.29   0 29   19 00   0 29   0 00   0 29   0 00   0 00   0 00   0 00       TOTAL LBMOL/HR   8525 10   6971 27   1553 83   6971 27   6478 78   1496.83   2,182 36   2,182 36   1179.02   1004.35       MASS FLOW LB/HR   160249   119227   41022   119227   105232   30726   35770   35770   19055   16732       VOLUME FLOW   78   63   —   —   59   —   20   —   11   —       MMSCFD       MOL MOLE, WT   18 80   17 10   26 40   17 10   16 24   20 53   16 39   16 39   16 16   16.66       DENSITY LB/FT 3     2 83   5 92   26 30   1.51   1.32   26 94   2 06   4 01   2 35   20 51       TEMPERATURE   120   −72   −72   −163   −178   −165   −132   −153   −153   −153       ° F.       PRESSURE PSIA   827.00   812 00   812 00   200 00   193 00   385 00   330 00   328 00   328 00   353 00                            Percent   Percent Recovered       STREAM   STREAM NUMBER   Recovered to   To Less Volatile            NAME   25   26   15   22   21   Volatile Fraction   Fraction               NITROGEN   0 00   0 00   0 00   0 00   99 17   100 00%   0 00%       CARBON DIOXIDE   0 00   0 00   6 33   6 33   2 31   26 71%   73 30%       METHANE   0 00   0.00   10 46   10 46   7543 46   99 87%   0 14%       ETHANE   0.00   0 00   473 61   473.61   12 79   2 63%   97 37%       PROPANE   0.00   0 00   198 24   198 24   0 07   0 04%   99 96%       I-BUTANE   0.00   0 00   36 66   36.66   0 00   0 00%   100 00%       N-BUTANE   0 00   0 00   63 30   63 30   0 00   0 00%   100 00%       I-PENTANE   0 00   0 00   20 83   20 83   0.00   0 00%   100 00%       N-PENTANE   0 00   0 00   20 63   20 63   0 00   0 00%   100 00%       HEXANE   0 00   0 00   19 29   19 29   0 00   0 00%   100 00%       TOTAL LBMOL/HR   0 00   0 00   868.31   868 31   7657 80       MASS FLOW LB/HR   0   0   35978   35978   124286       VOLUME FLOW MMSCFD   —   —   —   —   70       MOLE WT   16 66   16 66   41.44   41 44   16.23       DENSITY LB/FT 3     20.51   20 51   30 11   27.97   1.03       TEMPERATURE ° F.   −153   −153   71   100   167       PRESSURE PSIA   353 00   353 00   500 00   495 00   413 41                  
 
         [0045]    [0045]                                                                                                                           TABLE 1B                       THE PRO-QUIP CORPORATION                                STREAM   STREAM NUMBER            NAME   1   3   4   5   9   10   14   16   18   23               NITROGEN   345 88   280 87   65 02   280 87   275 89   16.91   19.90   84.91   69.99   11.93       CARBON   327 77   161 06   166 70   161.06   48 44   254.24   37.16   203 85   26 83   141.62       DIOXIDE       METHANE   24864 18   16379 96   8484 21   16379 96   17115 17   6530 39   8271 66   16754 42   7672.43   7265 60       ETHANE   3696 03   1309.26   2386 76   1309.26   179 47   3053 40   131 47   2518 25   113 74   1923.61       PROPANE   2012 72   363 60   1649 12   363 60   10 96   1673 25   11 09   1660 25   9 49   1320 61       I-BUTANE   385.41   40 55   344.87   40 55   0 43   316 09   0 54   345 41   0 46   275.96       N-BUTANE   612.71   50 73   561 98   50 73   035   500 03   0 49   562 47   0 41   449.65       I-PENTANE   151.53   7 05   144 48   7 05   0 02   122 62   0 03   144 51   0.03   115.59       N-PENTANE   115 29   4.29   111 00   4 29   0 01   93 09   0 01   111 02   0 01   88.80       HEXANE   98 82   1 67   97 15   1.67   0.00   79 39   0.00   97.15   0.00   77 72       HYDROGEN   0.00   0 00   0 00   0 00   0.00   0 00   0 00   0 00   0 00   0.00       SULFIDE       CARBONYL   3 29   0 68   2 61   0 68   0 03   2 74   0 03   2 64   0 03   2 09       SULFIDE       TOTAL   32613.64   18599.74   14013 90   18599 74   17630 77   12642 15   8472 40   22484 88   7893 41   11673 17       LBMOL/HR       MASS FLOW   708883   339451   369432   339451   290366   352036   139402   508812   130123   302951       LB/HR       VOLUME   297   169   —   —   161   —   77   —   72   —       FLOW       MMSCFD       MOLE. WT,   21 74   18.25   26.36   18 25   16.47   27.85   16 45   22 63   16.48   25.95       DENSITY   4 20   6 88   24.02   1.76   1.46   32.32   2 07   6 70   2.06   30.02       LB/FT 3         TEMP ° F.   120   −40   −40   −133   −149   −138   −129   −131   −131   −131       PRESSURE   978 00   966 35   966 35   242 00   237 00   375 00   335 00   330 00   330 00   370 00       PSIA                            Percent   Percent Recovered       STREAM   STREAM NUMBER   Recovered   To Less Volatile            NAME   25   26   15   22   21   to Volatile Fraction   Fraction               NITROGEN   2 98   2 98   0 00   0 00   345 88   100 00%   0 00%       CARBON DIOXIDE   35 40   35 40   252 48   252 48   75 27   22 97%   77 03%       METHANE   1816 40   1816 40   75 13   75 13   24787 60   99 69%   0 30%       ETHANE   480 90   480 90   3402 83   3402 83   293 21   7 93%   92 07%       PROPANE   330 15   330 15   1992 30   1992 30   20 46   1 02%   98 99%       I-BUTANE   68 99   68 99   384 53   384 53   0 89   0 23%   99 77%       N-BUTANE   112 41   112 41   611 95   611 95   0 76   0 12%   99 88%       I-PENTANE   28 90   28 90   151 49   151 49   0 04   0 03%   99 97%       N-PENTANE   22 20   22 20   115 28   115 28   0 02   0 02%   99 98%       HEXANE   19 43   19 43   98 82   98 82   0 00   0 00%   00 00%       HYDROGEN SULFIDE   0 00   0 00   0 00   0 00   0 00   0 00%   00 00%       CARBONYL SULFIDE   0 52   0 52   3 23   3 23   0 06   1 84%   98 16%       TOTAL LBMOL/HR   2918 29   2918 29   7088 04   7088 04   25524 18       MASS FLOW LB/HR   75738   75738   288372   288372   420489       VOLUME FLOW MMSCFD   —   —   —   232       MOLE WT   25 95   25 95   40 68   40 68   1647       DENSITY LB/FT 3     30 02   30 02   30 09   27 83   0 88       TEMPERATURE ° F.   −131   −131   72   100   115       PRESSURE PSIA   370 00   370 00   500 00   490 00   317 14                    
         [0046]    [0046]                                                                                                                           TABLE 2                       THE PRO-QUIP CORPORATION                                STREAM   STREAM NUMBER            NAME   1   3   4   5   9   10   14   16   18   23               HYDROGEN   1274.20   1203.16   71 03   1203 16   1200 28   3 85   29 12   75 29   73.92   0 96       NITROGEN   197 10   165 03   32 07   165 03   162 81   5 39   17 96   38 80   34.30   3.16       CARBON   13 01   10.54   2 47   10.54   10 36   0 52   1 53   3 13   2 65   0 34       MONOXIDE       METHANE   3194 56   1790 74   1403 81   1790 74   1992 70   641 30   1485 42   2397 90   1197 69   843.29       ETHYLENE   672 81   127 55   545 26   127.55   29 42   356 01   39 41   393 82   26 82   257.87       ETHANE   1402 52   155 95   1246 57   155 95   21 51   711 58   34 92   845 19   23 80   577 13       PROPENE   195 47   5.89   189.58   5.89   0.24   92 39   0 64   123 86   0.41   86.74       PROPANE   156.55   3 57   152 98   3 57   0 12   73 40   0 35   99 79   0 22   69 96       I-BUTANE   1 51   0 01   1 50   0 01   0 00   0 70   0 00   0 98   0 00   0.68       N-BUTANE   81 73   0 45   81 28   0.45   0 00   37 57   0 02   52 86   0 01   37 13       N-PENTANE   28 36   0.03   28.33   0.03   0 00   12.97   0.00   18 42   0 00   12 94       TOTAL LBMOL/HR   7217.81   3462.92   3754 89   3462 92   3417 45   1935 67   1609 35   4050 03   1359 84   1890.19       MASS FLOW LB/HR   142766   44774   97992   44774   40727   52131   26634   90329   21995   48083       VOLUME FLOW   66   32   —   —   31   —   15   —   12   —       MMSCFD       MOLE. WT   1978   12.93   26.10   12.93   11.92   26.93   16.55   22.30   16 10   25.44       DENSITY LB/FT 3     2 13   2 82   28 62   0.71   0.63   33 86   1 07   3 84   1 03   31 33       TEMPERATURE ° F.   100   −89   −89   −171   −183   −175   −146   −152   −152   −152       PRESSURE PSIA   581 00   726.00   726.00   148.60   145.00   213.00   185.00   181.00   181 00   213 00                            Percent   Percent Recovered       STREAM   STREAM NUMBER   Recovered to   To Less Volatile            NAME   25   26   15   22   21   Volatile Fraction   Fraction               HYDROGEN   0.41   0.41   0.00   0 00   1274 20   100 00%   0 00%       NITROGEN   1.34   1 34   0 00   0 00   197.11   100 00%   0 00%       CARBON MONOXIDE   0 14   0 14   0 00   0 00   13 01   100 00%   0 00%       METHANE   356.91   356.90   4.21   4.21   3190 39   99 87%   0 13%       ETHYLENE   109 14   109.14   616.58   616 58   56 24   8 36%   91 64%       ETHANE   244 26   244 27   1357 22   1357 22   45 32   3 23%   96.77%       PROPENE   36.71   36.71   194.82   194 82   0 65   0 33%   99 67%       PROPANE   29 61   29 61   156 21   156 21   0 34   0 22%   99.78%       I-BUTANE   0 29   0 29   1 51   1 51   0 00   0 00%   99 97%       N-BUTANE   15 71   15 71   81 71   81 71   0 02   0 02%   99 98%       N-PENTANE   5 48   5 48   28 36   28 36   0 00   0 00%   100 00%       TOTAL LBMOL/HR   800 00   800 00   2440 62   2440 62   4777 28       MASS FLOW LB/HR   20351   20351   80146   80146   62622       VOLUME FLOW MMSCFD   —   —   —   —   —       MOLE WT   25 44   25 44   32 84   32 84       DENSITY LB/FT 3     31 33   31 33   30 51   23 64       TEMPERATURE ° F.   −152   −152   −7   74       PRESSURE PSIA   213.00   213 00   585 00   580 00