Abstract:
This invention relates to a process for the manufacture of aromatic carboxylic acids by exothermic liquid phase oxidation of an aromatic feedstock. More particularly, this invention relates to the efficient energy recovery of the exotherm produced by the liquid phase oxidation of an aromatic feedstock. An apparatus useful in recovery of energy from the preparation of aromatic carboxylic acids by the exothermic liquid phase reaction of an aromatic feedstock is described where the primary means of energy recovery is by raising moderate pressure steam. This is coupled with a process to recovery low temperature energy using a process commonly known as an organic Rankine cycle and/or a heat pump. The combination of energy recovery methods increases the overall energy recovery and enables the recovery of reaction energy as either thermal energy (steam) or work or a combination of both.

Description:
FIELD OF THE INVENTION  
       [0001]     This invention relates to a process for the manufacture of an aromatic carboxylic acid-rich stream by exothermic liquid phase oxidation of an aromatic feedstock. More particularly, this invention relates to the efficient energy recovery of the exotherm produced by the liquid phase oxidation of an aromatic feedstock.  
       BACKGROUND OF THE INVENTION  
       [0002]     Aromatic carboxylic acids, such as terephthalic acid, isophthalic acid, and napthlene dicarboxylic acid are useful chemical compounds and are raw materials in the production of polyesters. In the instance of terephthalic acid, a single manufacturing facility can produce greater than 100,000 metric tons per annum as feedstock for a polyethylene terephthalate (PET) facility.  
         [0003]     Terephthalic acid (TPA) can be produced by the high pressure, exothermic oxidation of a suitable aromatic feedstock such as para-xylene. Typically, these oxidations are carried out in a liquid phase using air or alternate sources of molecular oxygen in the presence of a metal catalyst or promotor compound(s). Methods for oxidizing para-xylene and other aromatic compounds such as m-xylene and dimethyinaphthalene are well known in the art. These oxidation reactions will typically produce reaction gases generally comprising oxidation reaction products such as carbon monoxide, carbon dioxide, and methyl bromide. Additionally, if air is used as the oxygen source, the reaction gases may also contain nitrogen and excess oxygen.  
         [0004]     Most processes for the production of TPA also employ a low molecular weight carboxylic acid, such as acetic acid, as part of the reaction solvent. Additionally, some water is also present in the oxidation solvent as well as being formed as an oxidation by-product.  
         [0005]     Oxidations of this type are generally highly exothermic, and although there are many ways to control the temperature of these reactions, a common and convenient method is to remove the heat by allowing a portion of the solvent to vaporize during the reaction. The combination of the reaction gases and the vaporized solvent is referred to as a gaseous mixture. The gaseous mixture contains a considerable amount of energy.  
         [0006]     Because water is formed as an oxidation by-product, at least a portion of the gaseous mixture either as vapor or condensate is usually directed to a separation device, typically a distillation column, to separate the water from the primary solvent (e.g. acetic acid) so that the water concentration in the reactor is not allowed to build up.  
       SUMMARY OF THE INVENTION  
       [0007]     An objective of this invention is to provide a method for efficient and economical recovery of energy that is generated as a result of a highly exothermic oxidation reaction producing an aromatic carboxylic acid. Another objective of this invention is to provide for the energy recovery while simultaneously performing a chemical separation between a low molecular weight carboxylic acid solvent and water.  
         [0008]     In one embodiment of this invention, a process for recovery of thermal energy from an offgas stream is provided the process comprises the following steps: 
        a) oxidizing an aromatic feedstock with a liquid phase reaction mixture in a reaction zone to form an aromatic carboxylic acid-rich stream and a gaseous mixture;     b) removing in a separation zone a substantial portion of a solvent from the gaseous mixture to form the offgas stream and a solvent rich stream; and     c) recovering the thermal energy from at least a portion of the offgas stream in a heat recovery zone; wherein a portion of the offgas stream is condensed to form a condensed mixture; wherein the condensed mixture is optionally recycled back to the separation zone; wherein a portion of the thermal energy is recovered in a working fluid; and wherein a portion of the enthalpy in the working fluid is recovered in a power cycle; wherein the working fluid is a compound or mixture of compounds that have a normal boiling point between about −100° C. to about 90° C.        
 
         [0012]     In another embodiment of this invention, a process for recovery of thermal energy from an offgas stream is provided, the process comprises the following steps: 
        a) removing in a separation zone a substantial portion of an oxidation solvent from a gaseous mixture to form an offgas stream; and     b) optionally, recovering thermal energy from a portion of the offgas stream in a first heat recovery device to produce a low pressure steam.     c) recovering thermal energy from a portion of the offgas stream in a second heat recovery device utilizing a working fluid through a power cycle; wherein a portion of the enthalpy in the working fluid is recovered in a power cycle; wherein the working fluid is a compound or mixture of compounds that have a normal boiling point between about −100° C. to about 90° C.; and     d) optionally, recovering thermal energy from a portion of the offgas stream in a third heat recovery device.        
 
         [0017]     In yet another embodiment of this invention a process for recovery of thermal energy from an offgas stream is provided. The process comprises the following steps: 
        a) oxidizing an aromatic feedstock with a liquid phase reaction mixture in a reaction zone to form an aromatic carboxylic acid stream and a gaseous mixture;     b) removing in a separation zone a substantial portion of a solvent from the gaseous mixture to form an offgas stream; and     c) optionally, recovering thermal energy from a portion of the offgas stream in a first heat recovery device to produce a low pressure steam;     d) recovering thermal energy from a portion of the offgas stream in a second heat recovery device using a working fluid through a power cycle; wherein said working fluid is a compound or mixture of compounds that have a normal boiling point between about −100° C. to about 90° C.; and     e) optionally, recovering thermal energy from a portion of the offgas stream in a third heat recovery device.        
 
         [0023]     In yet another embodiment of this invention a process for recovery of thermal energy from an offgas stream is provided. The process comprises the following steps in the order named: 
        a) oxidizing an aromatic feedstock with a liquid phase reaction mixture in a reaction zone to form an aromatic carboxylic acid stream and a gaseous mixture;     b) removing in a separation zone a substantial portion of solvent from the gaseous mixture to form an offgas stream;     c) recovering thermal energy from a portion of the offgas stream in a first heat recovery device to produce a low pressure steam;     d) recovering thermal energy from a portion of the offgas stream in a second heat recovery device using a working fluid through a power cycle; wherein said working fluid is a compound or mixture of compounds that have a normal boiling point between about −100° C. to about 90° C.; and     e) recovering thermal energy from a portion of the offgas stream in a third heat recovery device.       
 
     
    
     BRIEF DESCRIPTION OF THE DRAWINGS  
       [0029]      FIG. 1  illustrates different embodiments of the invention where a process to produce thermal energy from an offgas stream is provided.  
         [0030]      FIG. 2  illustrates different embodiments of the invention where a process to produce thermal energy from an offgas stream is provided through the use of at least one device.  
         [0031]      FIG. 3  shows a typical “condensation curve” which describes the heat duty of a condenser or partial condenser as a function of temperature  FIG. 4  shows an example of a power recovery system. 
     
    
     DETAILED DESCRIPTION OF THE INVENTION  
       [0032]     In the first embodiment of this invention, a process for recovery of thermal energy from an offgas stream  145  is provided in  FIG. 1 . The process comprises the following steps.  
         [0033]     Step (a) comprises oxidizing an aromatic feedstock  105  with a liquid phase reaction mixture  110  in a reaction zone  115  to form an aromatic carboxylic acid-rich stream  120  and a gaseous mixture  125 .  
         [0034]     The liquid phase reaction mixture  110  comprises water, a solvent, a metal oxidation catalyst and a source of molecular oxygen. The reaction zone  115  comprises at least one oxidation reactor. The oxidizing is completed under reaction conditions which produce the aromatic carboxylic acid-rich stream  120  and the gaseous mixture  125 . Typically, the aromatic carboxylic acid-rich stream  120  is a crude terephthalic acid slurry.  
         [0035]     Crude terephthalic acid is conventionally made via the liquid phase air oxidation of paraxylene in the presence of a heavy metal oxidation catalyst. Suitable catalysts include, but are not limited to, cobalt, manganese and bromide compounds, which are soluble in the selected solvent. Suitable solvents include, but are not limited to, aliphatic mono-carboxylic acids, preferably containing 2 to 6 carbon atoms, or benzoic acid and mixtures thereof and mixtures of these compounds with water. Preferably the solvent is acetic acid mixed with water, in a ratio of about 5:1 to about 25:1, preferably between about 10:1 and about 15:1. However, it should be appreciated that other suitable solvents, such as those disclosed herein, may also be utilized. Conduit  125  contains a gaseous mixture which comprises vaporized solvent, gaseous by-products, nitrogen and unreacted nitrogen generated as a result of an exothermic liquid phase oxidation reaction of an aromatic to an aromatic carboxylic acid. Patents disclosing the production of terephthalic acid such as U.S. Pat. No. 4,158,738 and #3,996,271 are hereby incorporated by reference.  
         [0036]     Step (b) comprises removing in a separation zone  130  a substantial portion of a solvent from the gaseous mixture  125  to form the offgas stream  135  and a solvent rich stream  140 .  
         [0037]     The offgas stream  135  comprises water, gaseous by-products, and small amounts of solvent. When the solvent is a low molecular weight carboxylic acid solvent, the ratio of water to low molecular weight carboxylic acid solvent is in the range of about 80:20 to about 99.99:0.01 by mass. The gaseous by-products comprise oxygen, oxidation by-products, such as, carbon monoxide and carbon monoxide, and in the instance when air is used as a source of molecular oxygen, nitrogen. At least a portion of the offgas stream  135  or all of the offgas stream  135  is sent on to a heat recovery zone via conduit  145 .  
         [0038]     Typically, the temperature and pressure conditions of the offgas stream  145  are in the range of about 130 to about 220° C. and about 3.5 to about 18 barg. Preferably, the temperature and pressure conditions of the offgas stream  145  are in the range of about 90 to about 200° C. and about 4 to about 15 barg. Most preferably, the temperature and pressure conditions of the offgas stream  145  are in the range of about 130 to about 180° C. and about 4 to about 10 barg.  
         [0039]     The gaseous mixture in conduit  125  is directed to the separation zone  130 . Typically, the separation zone  130  comprises a high pressure distillation column having between about 20 and about 50 theoretical stages and a condenser or plurality of condensers. In the separation zone  130 , the solvent rich stream is recovered via conduit  140 . The purpose of the separation zone  130  is to perform a separation wherein at least a potion of the solvent is recovered and excess water is removed. In general, for the purposes of optimized energy recovery, there should be minimal pressure reduction between the contents of conduit  125  and conduit  135  and  145  since this represents a loss of potentially recoverable energy. Therefore, the separation zone  130  should operate at temperature and pressure conditions at or near that of the gaseous mixture from conduit  125 . At least a portion or all of the offgas stream  135  is sent to a heat recovery zone via conduit  145 , and the rest of the offgas stream  137  can be utilitized elsewhere within the process for producing the aromatic carboxylic acid.  
         [0040]     Step (c) comprises recovering the thermal energy from at least a portion of the offgas stream  145  in a heat recovery zone  150 . In the heat recovery zone  150 , a portion of the offgas stream  145  is condensed to form a condensed mixture  155 ; and the condensed mixture  155  can be optionally recycled back to the separation zone. A working fluid is utilized to recover the thermal energy. Generally the working fluid is a compound or mixture of compounds that have a normal boiling point between about −100° C. to about 90° C.  
         [0041]     The recovering of the thermal energy from the offgas stream  145  in a heat recovery zone  150  can be accomplished by any means known in the art. However, generally a power cycle is used. Power cycles are well known in the art. A power cycle is a cycle that takes heat and uses it to do work on the surroundings. There are numerous power cycles that are well known in the art. Examples of power cycles include, but are not limited to, an organic rankine cycle (ORC), a kalina cycle, or a power cycle as described in WO02/063141 herein incorporated by reference.  
         [0042]     Other examples of power cycles that can be used are disclosed in “A Review of Organic Rankine Cycles (ORCs) for the Recovery of Low-Grade Waste Heat” Energy, Vol. 22, No. 7, pp 661-667,1997, Elsevier Science Ltd, Great Britian and Absorption Power Cycles”, Energy, Vol. 21, No. 1, pp 21-27, 1996, Elsevier Science Ltd, Great Britain, are herein incorporated by reference.  
         [0043]     One common feature among these examples is the use of low temperature evaporating working fluids. Typically, low temperature evaporating working fluids are used in power cycles to recover thermal energy at relatively low temperatures (e.g. at temperatures generally below 150° C.) instead of water or steam due to the higher power recovery efficiencies. One such cycle is a rankine cycle that is characterized by an isothermal boiling/condensing process. Steam turbine plants usually closely approximate a rankine cycle process wherein the working fluid is substantially water. However, as commonly accepted, rankine cycle power recovery using water/steam at low temperatures (e.g. at temperatures generally below 150° C.) are generally inefficient.  
         [0044]     The working fluid can be any fluid as long as it is substantially free of water wherein substantially free is approximately less than 20% by weight.  
         [0045]     In another embodiment of the invention wherein the working fluid is a compound or mixture of compounds that have a normal boiling point between about −100° C. to about 90° C. Another range is the working fluid can be a compound or mixture of compounds that have a normal boiling point between about −100° C. to about 600° C.  
         [0046]     In another embodiment of the invention the working fluid is selected from the group consisting of propane, isopropane, isobutane, butane, isopentane, n-pentane, ammonia, R134a, R11, R12, and a mixtures thereof. R134a, R11, R12 are known in the art and commonly available commercial refrigerants.  
         [0047]     In a second embodiment of the invention, a process for recovering of thermal energy from at least a portion of an offgas stream  235  via conduit  245  is provided in  FIG. 2 . The process comprises the following steps.  
         [0048]     Step (a) removing in a separation zone  230  a substantial portion of a solvent from the gaseous mixture  225  to form the offgas stream  235  and a solvent rich stream  240 .  
         [0049]     Step (a) in the second embodiment is substantially the same as step (b) in the first embodiment of the invention. In the case where the separation zone comprises a distillation column, the offgas stream  245  exits the top of the distillation column through conduits  245  and  237 . The offgas stream  245  comprises gaseous reaction by-products, nitrogen, unreacted oxygen. The solvent, typically acetic acid and water are also present in amounts at or near saturation conditions. The ratio of water to acetic acid is roughly in the range of 80:20 to 99.99:0.01 by mass, preferably in the range of 99.5:0.5 to 98.5:1.5 by mass. A portion of this offgas stream, represented by the contents of conduit  245 , can be passed through a series of heat recovery zones,  260 ,  270 , and  280 . A portion of the offgas stream  145  is condensed and directed via conduit  255  either as reflux flow to the distillation column in the separation zone  230  via conduit  255  or as liquid distillate via conduit  285 .  
         [0050]     From a distillation perspective, the role of  260 ,  270 , and  280  is to condense enough material from the overhead offgas stream  245  to provide the distillation column in the separation zone  230  with adequate reflux to drive the solvent and water separation. However, the heat duty necessary to perform the condensation also serves to remove heat generated by the oxidation reaction of the aromatic feedstock to the aromatic carboxylic acid.  
         [0051]     It would be useful and efficient to recover the energy. One barrier to efficient energy recovery is due to the presence of non-condensable gases in conduits  245  and  237 . The non-condensable gases, for example, nitrogen, oxygen, carbon monoxide, and carbon dioxide, give rise to a condensation heat curve that is not amenable to producing steam.  
         [0052]     This is illustrated by the example in  FIG. 3 .  FIG. 3  shows a typical “condensation curve” which describes the heat duty of a condenser or partial condenser as a function of temperature. In this case, the condenser is a partial condenser with a vapor inlet temperature of about 139° C. and an outlet temperature of about 45° C.  
         [0053]     If it is desirable to produce about 15 psig steam or about 1 barg in a single partial condenser unit, then  FIG. 3  indicates that only 55% of the total duty of the condenser can be used to produce 15 psig steam. This is because 15 psig steam has a saturation temperature of about 121° C. In this example of a partial condenser only 55% of the total duty can be transferred to the steam at temperatures at or above 121° C. This illustrates what is commonly known in heat transfer technology as a temperature “pinch” and represents a thermodynamic limitation on the system.  
         [0054]     It is possible to recover more heat if the pressure (and temperature) of the steam generated is lowered. However, this is of limited value because in order to utilize the steam for heating purposes elsewhere within the carboxylic acid production process, the steam must be of sufficient temperature.  
         [0055]     Step (b) comprises optionally recovering thermal energy from a portion of the offgas stream  245  in a first heat recovery zone  260  to produce a low pressure steam; 
        Step (c) comprises recovering thermal energy from a portion of the offgas stream  245  in a second heat recovery zone  270  using a working fluid through a power cycle; wherein said working fluid is a compound or mixture of compounds that have a normal boiling point between about −100° C. to about 90° C.        
 
         [0057]     Step (d) comprises recovering thermal energy from a portion of the offgas stream  245  in a third heat recovery zone  280 .  
         [0058]     The purpose of step (b), step (c) and step (d)&#39;s is for the efficient recovery of thermal energy. The heat recovery zones  260 ,  270 , and  280  comprise at least one device wherein thermal energy from the offgas stream  145 , is recovered. The first heat recovery zone  260  comprises a heat recovery device or plurality of devices wherein the heat transfer is accomplished at a temperature greater than about 121° C. The second heat recovery zone  270  comprises a heat recovery device or plurality of devices wherein the heat transfer is accomplished about a temperature greater than 90° C. The third heat recovery zone  280  comprises a heat device or plurality of devices wherein the heat transfer is accomplished at a temperature greater than 25° C. The heat recovery devices can be any device known in the art.  
         [0059]     The relevance of the heat recovery temperatures is evident in the efficiency and usefulness of the heat recovered at those temperatures. For temperatures greater than about 121° C., it is possible to produce about 15 psig (about 1 barg) saturated steam that is useful in industrial applications, such as the manufacture of aromatic carboxylic acids, as a heat media. Although it is possible to produce greater amounts of steam at lower temperatures, the usefulness of such steam is limited. Further, utilization of steam as a heating media for transferring heat to a lower temperature fluid is extremely thermodynamically efficient.  
         [0060]     The first heat recovery zone  260  typically comprises, but not limited to a partial condenser.  
         [0061]     The second heat recovery zone  270  typically comprises, but not limited to, a heat transfer device such as a condenser or partial condenser transferring heat to a “working fluid”, usually a refrigerant compound or a hydrocarbon or mixture of hydrocarbons. For heat and energy recovery at temperatures near or greater than 90° C., several methods are known in the art.  
         [0062]     The working fluid can be any fluid as long as it is substantially free of water wherein substantially free is approximately less than 20% by weight. In another embodiment of the invention wherein the working fluid is a compound or mixture of compounds that have a normal boiling point between about −100° C. to about 90° C. Another range is the working fluid can be a compound or mixture of compounds that have a normal boiling point between about −100° C. to about 600° C.  
         [0063]     In another embodiment of the invention the working fluid is selected from the group consisting of propane, isopropane, isobutane, butane, isopentane, n-pentane, ammonia, R134a, R11, R12, and a mixtures thereof. R134a, R11, R12 are known in the art and commonly available commercial refrigerants.  
         [0064]     Examples of power cycles include, but are not limited to, an organic rankine cycle, a kalina cycle, or a power cycle as described in WO02/063141.  
         [0065]     The organic rankine cycle (ORC) which been shown to be effective and economical for recovery of mechanical work and/or electricity from industrial waste heat. Practically, due to the irreversibility of thermodynamic systems, it is impossible to convert all the available thermal energy into useful work. However, due to the limited usefulness of the low pressure steam, it is far more economically advantageous to recover the energy by some other means than raising steam.  
         [0066]     There are several examples of industrial processes that utilize an ORC system for energy recovery. The main advantage of the ORC is its superior ability in recovering waste heat with low to medium temperature. For ORC systems where recovering energy in the range of 90 to 120° C., the system has efficiencies in the range of 3 to 20%. System efficiency is defined as the total work derived from the ORC system divided by the total inlet waste heat. The primary factors in the determining system efficiency are the working temperatures for the waste heat stream, the condenser temperature and the thermodynamic properties of the working fluid.  
         [0067]     Alternatively, the second heat recovery zone  270  can serve to transfer heater to a heat pump system. A large number of heat pump systems are known in the art. Therefore, any system capable of efficient recovery of energy from low temperature heat is applicable.  
         [0068]     The third heat recovery zone  280  comprises a heat recovery device or plurality of devices wherein the heat transfer is accomplished at or near a temperature greater than 25° C. Typically, the third heat recovery zone  280  comprises a water or air-cooled condenser or partial condenser.  
         [0069]     In a third embodiment of the invention, a process for recovery of thermal energy from an offgas stream  235  is provided in  FIG. 2 . The process comprises the following steps.  
         [0070]     Step (a) comprises oxidizing an aromatic feedstock  205  with a liquid phase reaction mixture  210  in a reaction zone  215  to form an aromatic carboxylic acid-rich stream  220  and a gaseous mixture  225 .  
         [0071]     Step (a) in the third embodiment of this invention is the same as step (a) in the first embodiment.  
         [0072]     Step (b) comprises removing in a separation zone  230  a substantial portion of a solvent from the gaseous mixture  225  to form the offgas stream  235  and a solvent rich stream  240 .  
         [0073]     Step (b) in the third embodiment is substantially the same as step (b) in the first embodiment of the invention.  
         [0074]     Step (c) comprises optionally recovering thermal energy from a portion of the offgas stream  245  in a first heat recovery zone  260  to produce a low pressure steam;  
         [0075]     Step (d) comprises recovering thermal energy from a portion of the offgas stream  245  in a second heat recovery zone  270  using a working fluid in a power cycle; wherein said working fluid is a compound or mixture of compounds that have a normal boiling point between about −100° C. to about 90° C.; 
        Step (e) comprises recovering thermal energy from at least a portion of the offgas stream  245  in a third heat recovery zone  280 .        
 
         [0077]     Step (c), Step (d) and Step (e) in the third embodiment of the invention is substantially the same as Step (b), Step (c) and Step (d) respectively in the second embodiment of this invention.  
       EXAMPLE  
       [0078]     This invention can be further illustrated by the following example of preferred embodiments thereof, although it will be understood that this example is included merely for purposes of illustration and are not intended to limit the scope of the invention unless otherwise specifically indicated.  
         [0079]      FIG. 4  shows an example of a power recovery system. The temperature and pressures are consistent with a terephthaic acid production. In this system, the working fluid for the organic rankine cycle system is n-pentane. Results based on ASPEN Plus™ computer simulation are shown in Table 2. Specific details about the equipment use in the model are shown in Table 1. Note that in this example about 55% of the total duty is used to produce 15 psig steam. An additional 38% of the total duty employs an ORC system for enhanced energy recovery. The overall thermal efficiency of the ORC system is roughly about 7.3%. It is assumed that significant improvements can be made by optimizing the choice of “working fluid” and by optimizing temperature and pressure operating conditions of the ORC system.  
                               TABLE 1                                   Item   Description   Comment                           321   15 psig steam generator   Duty˜2.18 × 10 6  BTU/hr           322   Pentane evaporator   Duty˜1.53 × 10 6  BTU/hr           323   Heat Exchanger   Duty˜0.24 × 10 6  BTU/hr           500   Turbine   Work Generated˜44 hp           510   Condenser   Duty˜1.41 × 10 6  BTU/hr           520   Pump   Work Required˜1.4 hp                        
         [0080]    
       
         
               
               
               
               
               
               
               
               
               
               
               
               
             
               
               
               
               
               
               
               
               
               
               
               
               
             
           
               
                 TABLE 2 
               
               
                   
               
               
                   
               
               
                 Stream Name 
                 304 
                 305 
                 306 
                 307 
                 308 
                 309 
                 310 
                 501 
                 502 
                 503 
                 504 
               
               
                   
               
             
             
               
                   
               
             
          
           
               
                 Mass Flow lb/hr 
                   
                   
                   
                   
                   
                   
                   
                   
                   
                   
                   
               
               
                 NITROGEN 
                 5919 
                 5908 
                 11 
                 5886 
                 33 
                 0 
                 33 
                 0 
                 0 
                 0 
                 0 
               
               
                 OXYGEN 
                 270 
                 269 
                 1 
                 267 
                 3 
                 0 
                 3 
                 0 
                 0 
                 0 
                 0 
               
               
                 WATER 
                 3764 
                 1551 
                 2213 
                 322 
                 3442 
                 0 
                 3442 
                 0 
                 0 
                 0 
                 0 
               
               
                 HOAC 
                 47 
                 19 
                 28 
                 6 
                 41 
                 0 
                 41 
                 0 
                 0 
                 0 
                 0 
               
               
                 PENTANE 
                 0 
                 0 
                 0 
                 0 
                 0 
                 0 
                 0 
                 8400 
                 8400 
                 8400 
                 8400 
               
               
                 Total Flow lb/hr 
                 10000 
                 7748 
                 2252 
                 6481 
                 3519 
                 0 
                 3519 
                 8400 
                 8400 
                 8400 
                 8400 
               
               
                 Temperature C. 
                 150.0 
                 130.0 
                 130.0 
                 90.0 
                 90.0 
                   
                 50.0 
                 35.0 
                 73.2 
                 52.7 
                 34.6 
               
               
                 Pressure psi 
                 145.2 
                 144.2 
                 144.2 
                 143.2 
                 143.2 
                 141.2 
                 141.2 
                 44.3 
                 43.3 
                 15.0 
                 14.0 
               
               
                 Vapor Frac 
                 1 
                 1 
                 0 
                 1 
                 0 
                   
                 0 
                 0 
                 1 
                 1 
                 0 
               
               
                 Liquid Frac 
                 0 
                 0 
                 1 
                 0 
                 1 
                   
                 1 
                 1 
                 0 
                 0 
                 1