Abstract:
Methods for improving a gasification process for halogenated materials and in particular for producing useful end products such as anhydrous or highly concentrated hydrogen halides and/or synthesis gas, the methods including recycling water/hydrogen halide vapors and/or carbon dioxide to a gasification reactor.

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS  
       [0001]    This application is a continuation of U.S. patent application Ser. No. 09/566,183, filed May 5, 2000. 
     
    
     
       FIELD OF THE INVENTION  
         [0002]    The invention relates to apparatus and methods to be utilized for the gasification of halogenated materials, and in particular to apparatus and methods that efficiently produce useful end products such as anhydrous or highly concentrated hydrogen halide and/or synthesis gas.  
         BACKGROUND OF THE INVENTION  
         [0003]    Related inventions include a prior patent application for a Method and Apparatus for the Production of One or More Useful Products from Lesser Value Halogenated Materials, PCT international application PCT/US/98/26298, published 1 Jul. 1999, international publication number WO 99/32937. The PCT application discloses processes and apparatus for converting a feed that is substantially comprised of halogenated materials, especially by-product and waste chlorinated hydrocarbons as they are produced from a variety of chemical manufacturing processes, to one or more “higher value products” via a partial oxidation reforming step in a gasification reactor. Other related inventions include six co-filed applications for certain other aspects of the process for gasifying halogenated material, such aspects including apparatus and methods for reactor vessel designs, gasifier nozzle designs, controlling aerosols, producing high quality acids, particulate removal and quench vessel designs.  
           [0004]    A gasification reaction process for halogenated materials is a technology for consuming halogenated material byproducts and waste streams, most likely liquid chlorinated organic byproducts and waste streams, and for producing substantially useful products therefrom. Successful implementation of the technology may replace liquid thermal oxidation facilities which represent the current industry technique for treating such waste and byproduct streams. Gasification offers several advantages over thermal oxidation including more economic costs, reduced emissions and the capture of maximal chemical value from the feed stream constituents. Gasification is also more flexible than the competing technologies in that it has a significantly broader range of acceptable feedstock composition.  
           [0005]    In a gasification process for halogenated materials, a source of oxygen (in gaseous form) is mixed with a source of one or more halogenated material feeds (typically in liquid form and pre treated or pre processed if necessary or desirable), the mixture taking place in at least one gasification reactor to produce syngas. The syngas typically comprises a hydrogen halide, CO and H 2  with residual C, CO 2 , H 2 O and trace elements.  
           [0006]    Such gasification in a reactor occurs at partial oxidation conditions, i.e. at oxygen to fuel ratios that are substoichiometric with reference to complete combustion. Under such conditions carbon particles or soot can be formed as a side product. This soot requires additional capture and treatment steps downstream in the process, thereby decreasing the economic efficiency of the process as a whole. One goal of the instant invention is to operate the gasification process more optimally while managing parameters such as pressure, temperature, reactants and flow rates so that the production of C (carbon particles or soot), CO 2  and H 2 O is minimized. Higher oxygen to fuel ratios can reduce the formation of soot. However, oxygen to fuel ratios are limited by permissible flame temperatures.  
           [0007]    In various processes for gasifying essentially hydrocarbonaceous fuels or waste products, steam is known to be used as a gasifying agent. Under suitable conditions steam is known to react with carbon (or carbonaceous waste products or soot) to convert the carbon to carbon monoxide and the steam to hydrogen, both carbon monoxide and hydrogen being desirable products. Steam is also known to be used as a “moderator” in regard to several functions in the environment of gasifying hydrocarbonaceous materials. The addition of steam “moderates” flame temperatures, allowing higher oxygen to fuel ratios to be utilized. Higher oxygen to fuel ratios, as mentioned above, can reduce the formation of soot due to a higher partial pressure of oxygen.  
           [0008]    Steam is also known to be used in gasification processes for essentially hydrocabonaceous materials for adjusting the hydrogen to carbon monoxide ratio of a product synthesis gas to meet the requirements of downstream customers.  
           [0009]    In the process of the gasification of hydrocarbonaceous materials, however, unlike in the instant gasification process, excess water created by used steam can be purged as waste water from downstream unit operations with a near negligible loss of valued products. In the gasification process of halogenated organic materials, the situation is otherwise. While the addition of steam to the gasification reactor can have the same beneficial effects mentioned above (of reducing soot and allowing higher oxygen to fuel operating ratios and supplying additional hydrogen,) the addition of steam can be wasteful. If the halogenated organic gasification process includes the production of a hydrogen halide to an anhydrous form, or even to a highly concentrated aqueous solution, the purge of the excess water can result in the loss of valuable product. In both processes, excess steam or water must be purged from the system downstream to maintain a water balance. In the case of the production of anhydrous or concentrated hydrogen halides, the purge step contains a significant concentration of the hydrogen halide. This loss is in proportion to the amount of steam moderator furnished to the gasifier.  
           [0010]    The present invention teaches a method to close the water balance in the halogenated organic gasification process while significantly minimizing the loss of valuable hydrogen halide product in an aqueous purge. More particularly, a gasification process for halogenated materials, if separated hydrogen halide is anticipated to be sold as an anhydrous product or in a highly concentrated solution, includes a distillation step to separate hydrogen halide product from water (in particular from water absorbed when hydrogen halide gas passes through an absorber stage). The present invention teaches the use of a vapor side-draw from the distillation stage wherein water/hydrogen halide vapor is extracted and recycled to the gasifier as a “moderator” steam stream. The distillation system can be run at a pressure higher than the gasifier, thereby providing pressure to straightforwardly feed the extracted water/hydrogen halide vapor into the gasifier. Optionally, to help avoid liquid carryover in the “moderator” stream to the gasifier, the water/hydrogen halide vapor stream can be superheated with an appropriate heat source, such as steam, a heat transfer fluid, or the like.  
           [0011]    The recycled vapor from the distillation step is principally water vapor but contains significant amounts of hydrogen halide. The hydrogen halide recycles through the gasifier to be subject to recapture again in the hydrogen halide recovery stage. The water vapor or steam is primarily consumed via gas shift reactions and carbon consuming reactions, discussed above. In such manner, the water balance of the process is maintained or completed while also achieving the desired objective of soot reduction. A combination of steam as well as recycled vapor can be utilized in whatever ratio needed in order to match and achieve the process water balance, as necessary. Recycled vapor with or without steam can also be used to adjust H 2  to CO ratio of the product syngas.  
           [0012]    Moderator streams are typically supplied to a gasification reactor through a suitably designed burner for intimate and appropriate mixing of all reactants. Lipp et al. describes one such burner system in a co-filed and co-pending patent application entitled Method and Apparatus for a Feed Nozzle for a Gasification Reactor for Halogenated Materials.  
           [0013]    An alternate methodology of the present invention teaches the use of another moderator, either together with or in lieu of the water/hydrogen halide vapor moderator, for helping to drive and to maintain the water balance of the gasification reactor process. As discussed above, synthesis gas created from the gasification of halogenated organics contains carbon dioxide. Methods for the removal and capture of carbon dioxide from synthesis gas are known. Carbon dioxide has some of the same reforming tendencies as steam. That is, carbon dioxide reacts with carbon and soot particles to produce carbon monoxide at gasification conditions. It is another aspect of the present invention that the carbon dioxide produced in the synthesis gas reaction can be captured and recycled as an alternate or further moderator, augmenting or displacing steam. Some water vapors are produced due to the gas shift reaction, e.g. CO+H 2 O&lt;—&gt;CO 2 +H 2 . The use of carbon dioxide as a moderator and/or a combination of steam and carbon dioxide thus further allows the process water balance to be managed without purging or losing hydrogen halide in an aqueous discharge. It can also be used to adjust H 2  to CO ratio in the product syngas. Depending on the operating pressure of the carbon dioxide recovery system, carbon dioxide can be pressured back to a gasifier reactor or a compression operation can be included for pressurizing the CO 2  stream to suitable pressures for feed to the gasifier. Alternately, carbon dioxide can be purchased and stored as a commodity. Carbon dioxide, thus stored can be supplied at appropriate pressure to the gasifier.  
           [0014]    As discussed above, while it is known in current gasification practice for conventional hydrocarbonaceous materials to use steam, and to a lesser extent carbon dioxide, to minimize soot formation and to adjust hydrogen to carbon monoxide ratios in the product syngas for intended consumers, the instant invention improves upon the above in that the “moderator” is or can be a recycled process fluid. Such use of the recycled process fluid prevents loss otherwise of hydrogen halide mixed into a purged water vapor process fluid. Using a recycled water/hydrogen halide vapor as a moderator provides a means for controlling the water balance of the process with the additional advantage of minimizing the aqueous waste volume discharged from the plant and minimizing the loss of product. As a further advantage, by providing a method for managing water balance, using a recycled water/hydrogen halide vapor as a moderator permits the use of higher water addition rates to a hydrogen halide absorption column. Use of higher water addition rates to a hydrogen halide absorption column for the synthesis gas creates a higher recovery efficiency of hydrogen halide.  
           [0015]    Recycling the purged water/hydrogen halide vapor as a moderator should have the further advantage of also permitting efficient utilization of a wider array of feed stock compositions. That is, feed stocks with a lower halide content can be processed while still producing anhydrous or highly concentrated hydrogen halide product since the loss of hydrogen halide has been lowered. Said otherwise, without use of the water/hydrogen halide vapor as a recycled moderator in the gasification reactor, recovered aqueous hydrogen halide from low halide feed concentration materials might be unsuitable for anhydrous recovery because of the otherwise excessive halide loss through aqueous discharge.  
           [0016]    The instant invention has a further advantage of requiring no additional significant equipment, except perhaps a vapor superheater. Generation of the water/hydrogen halide vapor and its recycling can be easily integrated into the distilling system. Whether anhydrous or aqueous hydrogen halide product is desired, recycling water/hydrogen halide vapor from a distillation stage allows the production of more concentrated solutions by managing water balance without loss of product. Further, for feed stocks lean on hydrogen, the recycled water/hydrogen halide vapor serves as an additional source of hydrogen for converting all halide to a hydrogen halide component.  
         SUMMARY OF THE INVENTION  
         [0017]    The present invention offers improved methods for a gasification process for halogenated materials. The improvements include one or more of the following goals: increasing the efficiency of the process; increasing and/or maximizing the anhydrous hydrogen halide recovery; minimizing the aqueous discharge; and adjusting the H 2  to CO ratio.  
           [0018]    The present invention includes apparatus and methods for increasing the efficiency of a gasification process for halogenated materials. The invention in one embodiment includes removing water/hydrogen halide vapors from a distillation stage of a gasification process and recycling the vapor as a reactant and/or moderator feed to a gasification reactor stage of the process.  
           [0019]    The method includes managing pressure, temperature and flow rate of the water/hydrogen halide vapor to control water balance, to lower carbon particle soot output and to moderate flame temperature in the gasification reactor. The method and apparatus include alternately or additionally capturing carbon dioxide from synthesis gas produced by a gasification of halogenated materials, or otherwise securing carbon dioxide, and feeding the carbon dioxide as a reactant and/or moderator gas to a gasification reactor stage of the process. The carbon dioxide may be added in addition to or in lieu of a water/hydrogen halide vapor moderator. 
       
    
    
     BRIEF DESCRIPTION OF THE DRAWINGS  
       [0020]    A better understanding of the present invention can be obtained when the following detailed description of the preferred embodiment is considered in conjunction with the following drawings, in which:  
         [0021]    [0021]FIGS. 1A and 1B illustrate block flow diagrams for a gasification process for halogenated materials; FIG. 1A illustrates recycling water/hydrogen halide vapor while FIG. 1B illustrates recycling captured CO 2 .  
         [0022]    [0022]FIGS. 2A and 2B illustrate in more detail a gasifier stage for a gasification process of FIGS. 1.  
         [0023]    [0023]FIG. 3 illustrates a quench and solids removal stage of a gasification process of FIG. 1.  
         [0024]    [0024]FIGS. 4A and 4B illustrate an absorber and an aqueous acid cleanup stage of a gasification process of FIGS. 1.  
         [0025]    [0025]FIG. 5 illustrates an anhydrous distillation stage of a gasification process of FIGS. 1. 
     
    
       [0026]    Tables 1A and 1B illustrate a numerical simulation of a run of a gasification reactor for halogenated materials demonstrating sensitivity of the outlet gas composition to varying the moderator flow rate.  
         [0027]    Tables 2A, 2B and 2C illustrate parameters for a commercially available system for the capture of carbon dioxide from syngas.  
         [0028]    Tables 3A-3E show, from a mathematical model, heat and material balances, demonstrating balancing of the water across a plant by recycling of the water.  
       DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS  
       [0029]    An embodiment for a gasification process for halogenated materials is indicated in block diagram form in FIGS. 1A and 1B. FIG. 1A illustrates an embodiment of the process in which water/hydrogen halide vapors  530  (assumed for the purpose of the embodiment to be H 2 O/HCL) are recycled from a distillation unit  500  back to a gasifier  200 , in a first aspect of the present invention. FIG. 1B illustrates an embodiment of the invention wherein syngas produced from a gasifier  200  is finished in a gas finishing stage  700  and is further processed in a CO 2  recovery stage  700 ′, for carbon dioxide recovery and the carbon dioxide stream  730  is recycled back to gasifier  200 . Of course, a preferred embodiment could provide for both recycling of carbon dioxide and water/hydrogen halide vapors. Further, carbon dioxide could be purchased and/or stored as opposed to, or in addition to being captured in a recovery stage.  
         [0030]    More particularly, FIGS.  2 - 5  illustrate in more detail aspects of an embodiment of a gasification process for halogenated materials than are indicated in block diagram form in FIGS. 1A and 1B. Elements of FIGS. 2 and 5, in particular, will be discussed in detail to illustrate preferred embodiments of the instant invention and to place the instant invention in perspective.  
         [0031]    [0031]FIGS. 2A and 2B illustrate a gasifier  200  in accordance with a preferred embodiment. The particular gasifier design of FIGS. 2A and 2B has two stages, primary gasifier R- 200  and secondary gasifier R- 210  for converting a fuel comprised substantially of halogenated materials to reaction products including hydrogen halide and synthesis gas components. For the purpose of this discussion the halogenated material will be assumed to be comprised of chlorinated hydrocarbons (RCL&#39;s). In FIG. 2A, RCL liquid stream  144  is atomized in primary reactor R- 200  with a pure oxygen stream  290  and a steam stream  293 , both injected through a main burner or nozzle BL- 200 . In the harsh gasification environment inside gasification reactor R- 200 , the RCl components are partially oxidized and converted to synthesis gas (syngas) comprised primarily of carbon monoxide, hydrogen, hydrogen chloride, and of lesser amounts of water vapor and carbon dioxide, as well or of some undesirable side products such as soot or carbon. The syngas flows into secondary reactor R- 210  to allow all reactions to proceed to completion, thus yielding very high destruction efficiencies of all species and minimizing undesirable side products such as soot. The output is syngas stream  210 .  
         [0032]    Because of the corrosive nature of HCl, both as a hot, dry gas and as a condensed liquid, the reactor shells and connecting conduit are shown jacketed with a closed heat transfer fluid system for wall temperature control, as indicated in FIGS. 2A and 2B in combination, which system comprises the subject of a related invention, filed simultaneously hereto. FIG. 2B illustrates a temperature control fluid circulating system to control the temperature of a pressure vessel wall of a gasifier, the fluid flowing between a pressure vessel wall and a jacket.  
         [0033]    The primary gasifier R- 200  of the instant embodiment functions to atomize the liquid fuel, evaporate the liquid fuel, and thoroughly mix the fuel with oxygen, moderator, and hot reaction products. The gasifier burner or nozzle design forms the subject of a related invention, filed simultaneously hereto. The gasifier R- 200  of the preferred embodiment operates at approximately 1450° C. and 75 psig. These harsh conditions insure near complete conversion of all feed components.  
         [0034]    The reactions that take place in gasifier R- 200  are many and complex. The reaction pathways and kinetics are not completely defined nor understood. Indeed, for the numerous species that comprise the anticipated gasifier feeds, the multiple reactions and their kinetics for each will be somewhat different. However, because of the extreme operating conditions in the gasifier, the reactions can be fairly represented by the overall reactions as defined below, in a close approach to equilibrium for most species.  
         [0035]    RCl Partial Oxidation:  
         [0036]    Chlorinated organics are partially oxidized to CO, H 2  and HCl.  
         C v H w Cl y +( v/ 2)O 2 →( v )CO+[( w−y )/2]H 2 =( y )HCl  
         [0037]    However, since the gasifier operates with a slight excess of oxygen above this stoichiometry, further oxidation occurs. Water vapor and carbon dioxide can also participate as oxidizers at gasification conditions.  
         C v H w Cl y +CO 2 →( v+ 1)CO+[( w−y )/2)]H 2 +( y )HCl  
         C v H w Cl y +H 2 O→( v )CO+[1+( w−y )/2]H 2 +( y )HCl  
         [0038]    Further oxidation reactions:  
         CO+½O 2 →CO 2    
         H 2 +½O 2 →H 2 O  
         [0039]    The oxidation reactions with oxygen, including the reaction C v H w Cl y +(v/2)O 2 →(v)CO+[(w−y)/2]H 2 =(y)HCl, are highly exothermic, and thus provide the energy for driving the other reactions, maintaining the gasifier temperature as desired.  
         [0040]    Thermal Decomposition Reactions:  
         [0041]    In local fuel rich zones resulting from the less than perfect mixing inherent to any burner, thermal decomposition occurs in the absence of oxygen or oxidizing species.  
         C v H w Cl x →C r +( x )HCl+( v−r )CH 4   +[w−x− 4*( v−r )/2]H 2    
         [0042]    where C is soot, and methane CH 4  is the simplest hydrocarbon molecule which is quite stable.  
         [0043]    Gas Shift Reactions:  
         [0044]    CO+H 2 O⇄CO 2 +H 2 , classic gas shift reaction, driven primarily by gas composition, pressure and temperature have limited effect within the narrow opening range of the gasifier.  
         [0045]    CH 4 +H 2 O⇄CO+3H 2 , steam—methane reforming driven almost completely to the right at gasifier conditions.  
         [0046]    Soot is also subject to partial oxidation reactions as described in paragraph 1 above, excluding the chlorine atom.  
         [0047]    Other Reactions:  
         [0048]    Due to the low partial pressure of oxygen in the gasifier, essentially all halogens, including chlorine as shown above, equilibrate to the hydrogen halide.  
         [0049]    Operating temperature in the gasifiers R- 200  and R- 210  should not be allowed to drop below approximately 1350° C. Conversion efficiency is reduced at lower temperatures. Because of accelerated corrosion attack to the refractory system, the gasifier temperature should not be allowed to exceed 1500° C. Conversion efficiency is very high at 1450° C. and only limited gains are made at higher temperatures, not justifying the accelerated refractory corrosion. Preferably, no RCl or liquid fluid is introduced to the gasifier until it is preheated to an acceptable operating temperature. Reactor temperature is actually controlled on a cascade loop with oxygen/fuel ratio. As described above, the oxidation reactions provide the heat to drive reactor temperature. The 0 2 /fuel ratio will therefore be increased or decreased as necessary to adjust reactor temperature to the targeted value. This ratio must be carefully controlled because of the sensitivity in using pure oxygen where small increments can cause significant temperature changes. The control band must also be limited to approximately one-half of the stoichiometric oxygen/fuel ratio to insure that the flammable mixture (syngas) environment in the gasifier is always maintained in a reducing state. Hazardous deflagrations can occur if excess oxygen is introduced to the fuel rich reactor chamber. Target oxygen to fuel ratio for the base feedstock is 0.489 lb of oxygen per 1.0 lb of liquid fuel. This will of course vary as the feed composition changes and if moderator flow is varied.  
         [0050]    Not only steam stream  293  but also, or alternately, an HCl/water vapor mixture stream  530  from a desorber T- 510  (FIG. 5) can be used as moderator flow. The moderator flow can be used to temper the flame temperature of the pure oxygen/fuel burner. This moderator can also serve as a coolant flow for the burner. Depending on the heating value of the liquid fuel, pure oxygen and the fuel can operate at the target gasifier temperature with insufficient oxygen to complete the partial oxidation reactions. This results in decreased conversion efficiency, increased soot. To correct this deficiency, moderator flow can be increased, thus permitting additional oxygen while maintaining the target gasifier temperature within limits. Moderator flow can be increased until sufficient oxidant is present to complete the desired reactions. In practice this can be defined by the concentration of fully oxidized species in the exit gas. For example, CO 2  and H 2 O may be targeted to be no less than 1.0 volume % each in the exit gas, and values as high as 10-15% vol. may be acceptable for heavy sooting or poor converting feedstocks. Steam as a moderator flow should be limited as possible because it does put additional load on the plant water balance and decreases the concentration of aqueous HCl absorbed downstream.  
         [0051]    The burner BL- 200  is an integral and vital component of a primary gasifier. The discharge jet from the burner provides a momentum source for mixing in a primary gasifier. The main burner should atomize the liquid into this mixing jet. Target atomization performance might be defined as where 99% of the liquid volume is of a droplet size of 500 microns or smaller. This should provide for a sufficient liquid surface area enabling rapid evaporation of the fuel. Two mechanisms play a role in the atomization in preferred embodiments. The preferred embodiments form the subject of a co-filed patent application. In preferred embodiments, liquid is injected through an annular arrangement of orifices centered around a central oxygen discharge. Pressure drop through these orifices initiates coarse atomization of the discrete liquid jets. The orifices, and thus the liquid jets, are directed to intersect out in front of the face of the burner, or more specifically, along the axis of the oxygen discharge, and so intersect with the oxygen discharge jet. The oxygen discharge jet provides a primary energy source for atomization. Static pressure of the oxygen is converted to kinetic energy through the burner nozzle. Preferably the burner provides a supersonic nozzle and so achieves a maximal velocity. The velocity differential between gas and liquid provides an atomization energy which reduces the liquid jet to fine, discrete droplets. Moderator steam may also be mixed with the oxygen upstream of the burner in this particular operating mode. Oxygen to the gasifier is preferably preheated to 120° C. to offset the temperature drop as oxygen is expanded through a supersonic atomizing nozzle, thus increasing atomization efficiency.  
         [0052]    To avoid induction of hot reaction chamber products into a near pure oxygen jet immediately at a burner face, and to avoid the extreme temperature conditions which result, moderator, or some portion thereof, can be jetted into the gasifier as an annular film surrounding the oxygen/fuel jet. This “inert” layer tends to move the hot oxidizing zone out away from the face of the burner, thus reducing the heat flux and resulting temperatures on the burner face.  
         [0053]    [0053]FIG. 2B, as mentioned above, illustrates a temperature control fluid system for reactor vessel wells. This system forms the subject of a separate co-filed patent application. The system can operate to control the wall temperature of the pressure vessels to approximately 200° C., or safely above the dew point of HCl to avoid condensation and resulting in increased corrosion of the pressure vessel wall.  
         [0054]    [0054]FIGS. 3, 4A and  4 B illustrate a quench and solids removal stage  300  of a preferred embodiment of a gasification process and an absorber  400  and aqueous acid  450  cleanup stage of a preferred embodiment of a gasification process. The quench, solids removal absorber and cleanup stages of the preferred embodiment lead to an anhydrous distillation stage  500  of FIG. 5, which is of particular significance to the instant invention. The disclosures of FIGS. 3, 4A and  4 B are included for background purposes and clarification.  
         [0055]    [0055]FIG. 5 illustrates features of a preferred embodiment for an anhydrous distillation process for halogenated materials. The anhydrous distillation area  500  in general consists basically of a distillation system, including desorber T- 510 , with auxiliary equipment to desorb a hydrogen halide stream, treated herein as an HCl stream, from an aqueous (hydrogen halide) HCl stream. A desorber overheads stream  503  in the preferred embodiment of FIG. 5 should comprise essentially a saturated HCl stream (+99 vol. % HCl). This HCl stream  503  can be further processed in one or more condensors, E- 515  and E- 520 , and in an anhydrous HCl drying and compression area  600 , including an HCl drying tower T- 620 . Desorber bottoms from desorber T- 510 , stream  501 , should comprise an azeotropic (˜22 wt. % HCl) aqueous HCl stream which can be recycled to an HCl recovery absorber, illustrated as stream  554 , where it can be reconcentrated to target aqueous acid strength.  
         [0056]    A hydrogen chloride—water system is a highly non-ideal mixture. It forms an azeotrope at approximately 20.0 wt. % HCl at atmospheric pressure. Water has a higher activity coefficient above this concentration. The azeotrope shifts with pressure, decreasing (HCl concentration reference) as pressure increases. The azeotrope is approximately 16.6 wt. % at 59 psig. When an absorber bottoms stream,  483 ,  500 ′, enters a desorber T- 510  above the azeotropic concentration in the desorber, HCl is a volatile species and is fractionated overhead.  
         [0057]    In the preferred embodiment of FIG. 5, aqueous acid from storage illustrated as stream  483  and referenced in FIG. 4, can be cross exchanged with the bottoms stream  510  and fed to the HCl desorber T- 510 . The feed is preferably introduced between an upper and lower packed section. The HCl desorber can fractionate HCl overhead while discharging a weak aqueous HCl stream from the bottoms. At preferred base design conditions (100 psig, 45° C. from the secondary condenser E- 520 ) the overheads gas should be about 96 vol. % HCl, 0.12 vol. % H 20 , with small amounts of noncondensibles—primarily CO 2  and to a lesser extent N 2 . Essentially all of the noncondensibles should be driven overhead in the desorber. Column bottoms may operate at approximately 175° C., and an acid concentration of about 22 wt. % HCl could be expected. Condensed liquid from both a primary E- 515  and a secondary E- 520  condenser can be collected in a reflux drum D- 515  and pumped back as, column reflux. A knock-out drum D- 520  after the secondary condenser can also remove free liquid to help prevent its carryover into the anhydrous HCl drying system. The column reboiler E- 510  can be driven by 235 lb. steam. Condensate level on the stream (shell) side of the reboiler can be controlled to manipulate heat transfer surface area, and thus reboiler duty for the column.  
         [0058]    When producing anhydrous HCl, as per the present invention, the water balance is preferably closed by using a sidedraw vapor  514  from a desorber as a moderator for the gasifier. This vapor may be, for instance, about 59 wt % H 20  and 41 wt. % HCl. When operating in this mode, the delivery pressure to a gasifier dictates the operating pressure of the desorber, which is about 100 psig. If no sidedraw vapor is required for the gasifier, operating column pressure can be reduced to 65-75 psig. The advantage of a lower operating pressure is cooler bottoms temperature which results in lower corrosion and permeation rates for the equipment. Boiling HCl as may exist at the bottoms of the desorber can be very aggressive, and milder operating conditions are more favorable to equipment reliability. Bottoms temperature is preferably not allowed to exceed 185° C. due to limitations of the typical impregnated graphite materials of reboiler tubes and the typical Teflon linings for towers and piping.  
         [0059]    The bottoms liquid stream  510 , which is cross exchanged with a desorber feed, can be further cooled to approximately 40° C. (or by using cooling tower E- 550 , which may include use of even sea water) and directed on to a dilute acid drum D- 550 . This drum can serve as a surge volume for the weak acid, which can be pumped back to a middle section of an HCl absorber, illustrated as stream  554 , where it absorbs additional HCl. A small blowdown to an environmental area, illustrated as to neutralizer R- 810 , can be used to control contaminant concentrations if these undesirables (salts, metals, etc.) build up to unacceptable levels.  
         [0060]    The following example, produced by computer model, illustrates typical parameters of a gasification reactor process for halogenated materials.  
       EXAMPLE 1  
       [0061]    The following feeds streams are fed to a gasifier through an appropriate mixing nozzle:  
                                                             Chlorinated Organic Material   9037 kg/hr           Oxygen (99.5% v purity):   4419 kg/hr           Recycle Vapor or moderator:   4540 kg/hr            [58.8 wt % water vapor, 41.2 wt % hydrogen chloride]                  
 
         [0062]    The resulting gasification reactions result in a synthesis gas stream rich in hydrogen chloride.  
         [0063]    In a preferred embodiment of the present invention, referencing the above example, this stream would be cooled or quenched and passed through an absorption step where the hydrogen chloride is recovered in an aqueous solution. This aqueous solution would be forwarded to a distillation system whose principal purpose is to distill nearly water free hydrogen chloride as an overhead product. The distillation tower is preferably operated at a pressure sufficient to flow side-draw vapor through a superheater, through a control valve, and through a gasifier mixing nozzle. A vapor side-draw is preferably extracted from a “reboiler section” of a distillation tower at a flowrate to complete the plant water balance. For the above example this would be per the flowrate and composition described for a gasifier feed. The vapor is preferably passed through a superheating exchanger imparting typically 10-20° C. superheat to the vapor, to insure that no liquid droplets remain. This vapor would then be fed to a gasifier mixing nozzle as a moderator stream.  
         [0064]    Alternatively and/or in addition to the above system, a synthesis gas which has been absorbed free of bulk hydrogen chloride, as described above and illustrated as stream  418  in FIG. 4, passes through a finishing system  700 , FIG. 1B, where essentially all hydrogen chloride and other contaminants are recovered. This clean synthesis gas can then be fed to a commercially available carbon dioxide removal system, illustrated as unit  700 ′ in FIG. 1B. Carbon dioxide can be absorbed, as is known, from the syngas, liberated from any solvent or sorbent, compressed if necessary, and fed back to a gasifier feed nozzle as stream  730  in FIG. 1B, also as a moderator.  
         [0065]    [0065]FIG. 1B, discussed initially, illustrates in block flow diagram form the addition of a carbon dioxide recovery unit  700 ′ after syngas finishing unit  700 . Tables  2 A,  2 B and  2 C illustrate a mathematical model run of a prior art carbon dioxide recovery unit and illustrate that it is known to recover CO 2  from syngas streams. FIG. 1B also illustrates a CO 2  recycle stream  730  recycled back and fed to a gasifier  200 . The CO 2  would preferably be fed through a nozzle or burner in a passageway provided for an inert gas moderator, such as steam.  
         [0066]    Tables 1A and 1B illustrate the mole fractions of exit gas from the secondary reactor of FIG. 2 in a model run upon varying the moderator flow rate. The tables chart the breakdown of stream  210  when using a hydrogen halide/steam recycle moderator. The flow rate in lbs/hr of the moderator stream was varied from 2,000 lbs/hr to 20,000 lbs/hr. Results by mathematical model were computed with and without a nitrogen purge. Note the increased oxygen content as evidenced by decreasing CO 2  and H 2 O concentrations as recycled vapor moderator flow is increased. The higher concentrations support the formation of soot. Another key factor to note for the operation is the decreasing fraction of HCN and MCBZ, for the various moderator flows, indicating more complete destruction of undesirable species as the moderator flow increased.  
         [0067]    Tables 3A-3E illustrate, from a mathematical model, the composition of various streams indicated in FIG. 2—FIG. 5 for a sample run. The heat and material balances demonstrate balancing of the water across the plant by recycling of the water.  
         [0068]    The foregoing disclosure and description of the invention are illustrative and explanatory thereof, and various changes in the size, shape, and materials, as well as in the details of the illustrated system may be made without departing from the spirit of the invention. The invention is claimed using terminology that depends upon a historic presumption that recitation of a single element covers one or more, and recitation of two elements covers two or more, and the like.  
                                                                                             Exit Gas From Secondary Reactor (Stream #210) using HCI/Steam recycle Moderator                                Basis:   6-30-99 RCI feed slate           HCI/steam recycle from Desorber as moderator fluid           O2/Fuel varied to control primary gasifier to 1450 C           1.5 MM Btu/hr heat loss from primary           1.5 MM Btu/hr heat loss from secondary           1000 #/hr N2 purge flow (except if noted)           75 psig operating pressure            Aspen File Folder:   \Gasifier with recycle HCI vapor\                                2,000           5,000                           No 2           No N2       Moderator Flow (#/hr)   2,000   purge   3,000   5,000   purge   10,000   15,000   20,000               Substream: MIXED       Mole Frac       WATER   9.43E-06   3.51E−06   1.07E−02   4.54E−02   4.36E−02   1.24E−01   0.190369   0.246732       N2   0.022592   0.000138   0.027186   0.025582   0.001352   0.0223   0.019777   0.017778       O2   0.00E+00   9.39E−21   5.87E−14   1.25E−12   1.03E−12   1.38E−11   4.60E−11   1.06E−10       CO2   6.76E−06   2.41E−06   7.10E−03   2.72E−02   2.60E−02   6.13E−02   0.081936   0.095095       CO   0.496939   0.50605   0.479269   0.429943   0.442537   0.336036   0.2695   0.219925       H2   0.211813   0.219081   0.220143   0.216676   0.224961   0.201889   0.184427   0.166906       HCL   0.249677   0.259451   0.249226   0.249262   0.25546   0.249337   0.2494   0.249446       CL2   6.83E−08   8.51E−08   6.74E−08   7.22E−08   7.20E−08   8.53E−08   9.95E−08   1.15E−07       CL   1.54E−05   1.94E−05   1.56E−05   1.68E−05   1.66E−05   1.94E−05   2.18E−05   2.42E−05       CH4   6.59E−03   6.98E−03   6.30E−03   5.92E−03   6.07E−03   5.15E−03   0.0045531   0.004081       HCN   0.011664   2.60E−03   1.15E−05   2.30E−06   6.00E−07   5.51E−07   2.36E−07   1.21E−07       NH3   3.72E−06   2.90E−07   4.29E−06   4.00E−06   9.76E−07   3.26E−06   2.63E−06   2.12E−06       FORMHYDE   4.77E−07   4.97E−07   4.77E−07   4.20E−07   4.49E−07   3.04E−07   2.22E−07   1.64E−07       NAPTHALN   1.30E−08   1.37E−08   1.24E−08   1.16E−08   1.19E−08   1.01E−08   8.95E−09   8.03E−09       C2HCL5   2.12E−22   2.08E−21   1.53E−28   7.04E−30   0.00E+00   6.03E−31   1.69E−31   6.85E−32       C2H2CL4U   3.43E−18   3.01E−17   2.54E−24   1.11E−25   0.002+00   8.39E−27   0.00E+00   0.00E+00       PERCHLOR   3.65E−16   3.52E−15   2.65E−22   1.23E−23   0.00E+00   1.06E−24   3.01E−25   1.23E−25       CCL4   1.41E−16   5.04E−16   1.17E−19   2.63E−20   0.00E+01   8.77E−21   5.30E−21   3.83E−21       C2H2CL4S   8.06E−18   7.07E−17   5.96E−24   2.61E−25   3.44E−25   1.97E−26   0.00E+00   0.00E+00       TCE   5.20E−12   4.58E−11   3.87E−18   1.72E−19   0.00E+00   1.33E−20   0.00E+00   0.00E+00       C2H3CL3   5.16E−14   4.11E−13   3.91E−20   1.64E−21   0.00E+00   1.10E−22   0.00E+00   0.00E+00       C2CL6   1.17E−26   1.27E−25   8.25E−33   0.00E+00   0.00E+00   0.00E+00   1.23E−35   5.65E−35       PDC   4.48E−13   8.20E−12   3.12E−22   2.46E−24   3.94E−24   3.36E−26   0.00E+00   0.00E+00       EPI   9.57E−19   7.38E−18   7.54E−25   2.71E−26   3.86E−26   1.20E−27   0.00E+00   0.00E+00       DCIPE   5.12E−30   6.03E−28   0.00E+00   0.00E+00   0.00E+00   0.00E+00   0   0       2M2P   1.65E−16   1.88E−14   9.24E−32   0.00E+00   0.00E+00   0.00E+00   0.00E+00   0       123TCP   3.20E−16   6.33E−15   2.17E−25   1.78E−27   0.00E+00   2.70E−29   0.00E+00   0.00E+00       PROPANAL   1.31E−11   8.57E−11   1.04E−17   3.53E−19   0.00E+00   1.34E−20   0.00E+00   0.00E+00       ACETONE   1.77E−11   1.11E−10   1.41E−17   4.70E−19   0.00E+00   1.74E−20   0.00E+00   0.00E+00       BENZENE   2.13E−08   2.25E−08   2.03E−08   1.91E−08   1.91E−08   1.66E−08   1.47E−08   1.32E−08       33DCPENE   1.73E−11   3.48E−10   1.18E−20   9.87E−23   1.51E−22   1.55E−24   0.00E+00   0.00E+00       13DCPENE   9.42E−11   1.87E−09   6.43E−20   5.34E−22   0.00E+00   8.32E−24   0.00E+00   0.00E+00       HXCLBZ   9.29E−23   4.33E−20   0.00E+00   0.00E+00   0.00E+00   0.00E+00   0   0       NCL3   0   7.62E−27   6.08E−26   7.07E−26   1.59E−26   9.71E−26   1.26E−25   1.59E−25       3CLACN   1.65E−13   3.10E−13   1.16E−22   1.05E−24   0.00E+00   2.06E−26   0.00E+00   0.00E+00       1-3BCH   3.76E−21   6.31E−20   2.67E−30   1.76E−32   0.00E+00   0.00E+00   0.00E+00   0       1-2BCH   1.51E−20   2.55E−19   1.08E−29   7.10E−32   0.00E+00   0.00E+00   0.00E+00   0       2-3DCBUT   9.16E−16   4.18E−14   5.70E−28   8.79E−31   1.65E−30   0.00E+00   0.00E+00   0       C4CL6   8.80E−30   6.65E−28   0.00E−00   0.00E+00   0.00E+00   0.00E+00   0   0       SIO2   0   0   0   0   0   0   0   0       SOOT   0   0   0   0   0   0   0   0       BO   1.13E−18   2.02E−17   8.20E−28   5.57E−30   0.00E+00   5.06E−32   0.00E+00   0.00E+00       BGLYCOL   7.88E−26   4.80E−25   6.40E−32   1.79E−33   0.00E+00   0.00E+00   0.00E+00   0       BUTANAL   8.23E−15   1.35E−13   5.88E−24   3.88E−26   6.63E−26   3.37E−28   0.00E+00   0.00E+00       IPROPCL   7.01E−11   1.18E−09   5.02E−20   3.81E−22   0.00E+00   4.63E−24   0.00E+00   0.00E+00       PROPCL   9.59E−11   1.63E−09   6.88E−20   5.24E−22   8.54E−22   6.41E−24   4.56E−25   5.62E−26                  
 
         [0069]    [0069]                                                                       2,000           5,000                           No N2           No N2       Moderator Flow (#/hr)   2,000   purge   3,000   5,000   purge   10,000   15,000   20,000                   Substream: MIXED                                       Mole Frac       2CLPENE   3.95E−08   7.24E−07   2.78E−17   2.22E−19   0.00E+00   3.08E−21   0.00E+00   0.00E+00       PHENPROP   9.45E−19   1.67E−15   0.00E+00   0.00E+00   0.00E+00   0.00E+00   0   0       MPK   1.18E−11   8.41E−09   4.79E−33   0.00E+00   0.00E+00   0.00E+00   0.00E+00   0       PHENOL   5.82E−10   6.36E−08   3.03E−25   8.48E−29   0.00E+00   5.19E−32   0.00E+00   0.00E+00       AMS   1.25E−08   6.07E−05   4.13E−35   0.00E+00   0.00E+00   0.00E+00   0   0       ODCB   1.12E−08   3.72E−06   5.00E−27   3.43E−31   0.00E+00   0.00E+00   0.00E+00   0.00E+00       PARADOW   1.02E−08   3.35E−06   4.52E−27   3.10E−31   0.00E+00   0.00E+00   0.00E+00   0.00E+00       MCBZ   1.60E−05   4.89E−03   7.33E−24   4.84E−28   0.00E+00   0.00E+00   0.00E+00   0.00E+00       PYRENE   8.21E−09   8.70E−09   7.85E−09   7.38E−09   7.56E−09   6.42E−09   5.67E−09   5.09E−09       133TCPEN   3.64E−14   7.80E−13   2.41E−23   2.08E−25   0.00E+00   3.61E−27   0.00E+00   0.00E+00       ALLYL-CL   4.41E−08   1.24E−07   3.11E−17   2.50E−19   3.88E−19   3.51E−21   0.00E+00   0.00E+00       CBE   0   0   0   0   0   0   0   0       PHENBUTE   8.33E−12   1.01E−07   0.00E+00   0.00E+00   0.00E+00   0.00E+00   0   0       DPHENMP   0.00E+00   7.46E−15   0.00E+00   0.00E+00   0.00E+00   000E+001   0   0       HBR   0   0   0   0   0   0   0   0       BR2   0   0   0   0   0   0   0   0       SICL4   6.53E−04   6.91E−04   2.33E−07   1.34E−09   1.58E−08   1.88E−09   8.25E−10   5.03E−10       FE2O3   0   0   0   0   0   0   0   0       FECL3   5.06E−06   5.36E−06   4.84E−06   4.55E−06   4.66E−06   3.96E−06   3.50E−06   3.14E−06       AL2O3   0   0   0   0   0   0   0       ALCL3   7.93E−06   8.40E−06   7.58E−06   7.13E−06   7.30E−06   6.20E−06   3.70E−06   2.60E−06       CAO   0   0   0   0   0   0   0   0       CACL2   7.21E−06   7.63E−06   6.89E−06   6.48E−06   6.64E−06   6.63E−06   4.98E−06   4.46E−06       BR   0   0   0   0   0   0   0   0       23DCPENE   1.99E−10   3.92E−09   1.36E−19   1.12E−21   0.00E+00   1.74E−23   0.00E+00   0.00E+00       22DCP   6.83E−14   1.24E−12   4.75E−23   3.74E−25   6.00E−25   5.08E−27   0.00E+00   0.00E+00       C5CL5N   4.79E−24   6.55E−23   0.00E+00   0.00E+00   0.00E+00   0.00E+00   0   0       C5H2CL3N   6.57E−16   7.58E−15   3.57E−31   0.00E+00   0.00E+00   0.00E+00   0.00E+00   0       C5HCL4N   2.94E−20   3.71E−19   1.55E−35   0.00E+00   0.00E+00   0.00E+00   0   0       DICLCNPY   3.25E−15   7.59E−15   1.72E−33   0.00E+00   0.00E+00   0.00E+00   0   0       BISETHER   0   0   0   0   0   0   0   0       ACROLEIN   1.27E−08   8.94E−08   9.94E−15   3.52E−16   0.00E+00   1.52E−17   0.00E+00;   0.00E+00       CL2PNOL   4.86E−20   3.50E−19   3.76E−26   1.31E−27   1.93E−27   5.49E−29   0.00E+00   0.00E+00       CH2CL2   2.72E−08   7.96E−08   2.37E−11   4.89E−12   5.73E−12   1.28E−12   6.00E−13   3.38E−13       Total Flow lb mol/hr   1321.261   1247.963   1381.906   1470.352   1434.68   1691.44   1912.531   2133.624       Total Flow lb/hr   32529.66   31126.74   33617.81   35871.65   34762.16   41528.93   47199.24   52887.04       Total Flow gal/min   58921.15   56368.69   61749.02   65956.6   64290.43   76400.18   86786.61   97143.3       Temperature C.   1376.724   1397.981   1380.072   1386.49   1384.792   1397.981   1405.718   1411.342       Pressure psig   74.5   74.5   74.5   74.5   74.5   74.5   74.5   74.5       Vapor Frac   1   1   1   1   1   1   1   1       Liquid Frac   0   0   0   0   0   0   0   0       Solid Frac   0   0   0   0   0   0   0   0       Enthalpy Btu/lb mol   −14478.5   −14979.1   −16364   −20516.2   −21031.3   −29004.8   −35508.6   −40677.4       Enthalpy Btu/lb   −588.075   −600.556   −672.665   −840.944   −867.99   −1181.34   −1438.82   −1641.05       Enthalpy Btu/hr   −1.91E+07   −1.87E+07   −2.26E+07   −3.02E+07   −3.02E+07   −4.91E+07   −6.8E+07   −8.7E+07       Entropy Btu/lb mol-R   22.80366   22.93713   22.34239   21.53223   21.63093   19.6209   18.02903   16.70795       Entropy Btu/lb-R   0.926219   0.919617   0.918414   0.88259   0.892736   0.799144   0.730543   0.67405       Density lb mol/cu ft   2.80E−03   2.76E−03   2.79E−03   2.78E−03   2.78E−03   2.76E−03   0.002747   0.002738       Density lb/cu ft   0.068832   0.068846   0.067877   0.067807   0.061413   0.06777   0.067805   0.067876       Average MW   24.62016   24.94203   24.32713   24.39665   24.22991   24.55241   24.67894   24.78743                    
         [0070]    [0070]                                                                                                     GLOBAL GAS/SPEC TECHNOLOGY GROUP AMINE PLANT PROGRAM                                DATE:   16 DEC. 1999   SALES:       STC NUMBER:   99438UU   RUN BY: DUPART       COMPANY:   DOW       PLANT NAME:   SYN GAS       PLANT LOCATION:   MIDLAND       RESULTS GIVEN TO:   HENLEY       SOLVENT TYPE:   MEA       TREATED GAS REQUESTED.   95+% PURITY HYDROGEN            INLET GAS                12.800   MMSCFD,(DRY)   0.000%   H2S           100   Deg F.   38.013%   CO2           74.7   Psia   0.000%   CH4                   0.000%   C2H6                   0.000%   C3H8                   0.000%   i-C4H10                   0.000%   n-C4H10                   0.000%   i-C5H12                   0.000%   n-C5H12                   0.000%   C6H14                   0.000%   C7H16+                   0.000%   Ar                   0.000%   CO                   0.000%   N2                   60.723%   H2                   1.264%   H2O            RUN CONDITIONS            TREATED GAS H2S CONCENTRATION, WET BASIS   0.00   PPMV               TREATED GAS CO2 CONCENTRATION, WET BASIS   0.1476   VOL %       BAROMETRIC PRESSURE   14.70   Psia       ABSORBER BOTTOM PRESSURE   74.70   Psia       ABSORBER LEAN AMINE FEED TEMPERATURE   110   F.       ABSORBER OVERHEAD TEMPERATURE   218   F.       ABSORBER BOTTOMS TEMPERATURE   136   F.       STRIPPER BOTTOMS PRESSURE   12.00   Psig       STRIPPER REFLUX RATIO   2.00   Mol/Mol       STRIPPER OVERHEAD TEMPERATURE   218   F.       STRIPPER FEED TEMPERATURE   205   F.       STRIPPER BOTTOMS TEMPERATURE   246   F.       ACID GAS TEMPERATURE EXITING CONDENSER   120   F.       LEAN COOLER INLET TEMPERATURE   176   F.       COOLING WATER INLET/OUTLET   90   F.   110   F.       AIR COOLING INLET/OUTLET   90   F.   110   F.                    
         [0071]    [0071]                                                                                                                                                                             GLOBAL GAS/SPEC TECHNOLOGY GROUP PLANT PROGRAM                   AMINE VARIABLES                CO2 LEAN SOLVENT LOADING   0.100   Mol/Mol           CO2 NET SOLVENT LOADING   0.251   Mol/Mol           CO2 GROSS SOLVENT LOADING   0.351   Mol/Mol           H2S LEAN SOLVENT LOADING   0.000   Mol/Mol           H2S NET SOLVENT LOADING   0.000   Mol/Mol           H2S GROSS SOLVENT LOADING   0.000   Mol/Mol           SOLVENT CONCENTRATION   15   wt %           SOLVENT CIRCULATION RATE   1750.0   USGPM            GAS FLOW/PERFORMANCE DATA                INLET CO2 PARTIAL PRESSURE   1487.29   mmHg               INLET H2S PARTIAL PRESSURE   0.00   mmHg           NET CO2 REMOVAL   539.91   lbmole/hr           NET H2S REMOVAL   0.00   lbmole/hr           PERCENT CO2 REMOVED/SLIPPED   99.76   /   0.24            ENERGY BALANCE                REBOILER DUTY   77.684   MMBTU/hr           STRIPPER CONDENSER DUTY   22.069   MMBTU/hr           CROSS EXCHANGER DUTY   60.428   MMBTU/hr           LEAN SOLVENT COOLER DUTY   56.351   MMBTU/hr           UNIT REBOILER DUTY   143884   BTU/lbmole A G.            ESTIMATED EQUIPMENT SIZES            ABSORBER DIAMETER (ESTIMATE FOR TRAYED)   7.6   ft                   ABSORBER TRAY SPACING/No. OF TRAYS   24   in       /   20       ABSORBER DIAMETER: 1.5 IN. METAL PALL RINGS   5.6   ft       CARBON: (% Slip/Vol. (ft{circumflex over ( )}3)/Dia. (ft))   10   /   467.88   /   7.46       STRIPPER DIAMETER (ESTIMATE FOR TRAYED)   13.0   ft       STRIPPER TRAY SPACING/No. OF TRAYS   24   in       /   20       STRIPPER DIAMETER: 1.5 IN. METAL PALL RINGS   9.5   ft                    HEAT EXCHANGE EQUIPMENT:   AREA (ft{circumflex over ( )}2)   LMTD (F)   Uo (BTU/hr*ft{circumflex over ( )}2*F)                   CROSS EXCHANGER   12434   40.5   120       REBOILER   9996   51.8   150       LEAN COOLER (WATER)   11278   38.4   130       LEAN COOLER (AIR)   13329   38.4   110       REFLUX CONDENSER (WATER)   3297   60.8   110       REFLUX CONDENSER (AIR)   4836   60.8    75            LEAN COOLER H2O (USGM)   5640.7   LEAN COOLER FAN (hp)   435.0       REFL. COND. H2O (USGPM)   2204.6   REFL. COND. FAN (hp)   170.3                    
         [0072]    [0072]                                                                     GLOBAL GAS/SPEC TECHNOLOGY       GROUP AMINE PLANT PROGRAM                   PUMPING EQUIPMENT ESTIMATES                        AMINE CHARGE PUMP (P.D.)    68.07 hp           AMINE CHARGE PUMP (CENTR.)   102.10 hp           AMINE BOOSTER PUMP   105.00 hp           REFLUX WATER PUMP    2.26 hp                        STREAM CONDITIONS                INLET   SALES   ACID       GAS STREAMS (lbmole/hr)   GAS   GAS   GAS               TEMPERATURE, Deg F.   100   110   120       PRESSURE, Psia   74.70   72.70   22.70       Ar   0.00   0.00   0.00       H2   864.52   862.92   1.60       N2   0.00   0.00   0.00       CO   0.00   0.00   0.00       CH4   0.00   0.00   0.00       C2H6   0.00   0.00   0.00       C3H8   0.00   0.00   0.00       C4H10+   0.00   0.00   0.00       CO2   541.21   1.30   539.91       H2S   0.00   0.0000   0.00       H2O   18.00   15.41   43.34       TOTAL (lbmole/hr)   1423.72   879.64   564.84       TOTAL (M lb/hr)   25.89   2.07   24.55       DENSITY (lb/ft{circumflex over ( )}3)   0.222   0.029   0.154       ACTUAL ft{circumflex over ( )}3/min   1942.10   1210.90   2664.27                   LEAN   RICH       SOLVENT STREAMS (lbmol/hr)   AMINE   AMINE               TEMPERATURE, Deg F.   110   136       PRESSURE, Psia   72.7   74.7       Ar   0.00   0.00       H2   0.00   1.60       N2   0.00   0.00       CO   0.00   0.00       CH4   0.00   0.00       C2H6   0.00   0.00       C3H8   0.00   0.00       C4H10+   0.00   0.00       CO2   214.71   754.62       H2S   0.00   0.00       H2O   41254.34   41256.92       MEA   2147.09   2147.09       TOTAL (lbmole/hr)   43616.14   44160.23       TOTAL (M lb/hr)   883.80   907.63       DENSITY (lb/ft{circumflex over ( )}3)   62.96   64.20       USGPM   1750.00   1762.54       USGPM   MAKE-UP   RE FLUX           H2O   FLOW           1.47   37.72                    
         [0073]    [0073]                                                                                           Stream Number:   144   200   210   280   281   282   285   290   291   293   295   296   299   530   733       To:   R-3200   R-3210       P-3280   R-4   E-3280   D-3280   E-3200   R-3200   R-3200   R-3200   R-3206   E-3280   R-3200   R-3200       From   E-31-10   R-3200   D-3280   P-3280   Q3200   E-3280       E-3280           LIQUID   VAPOR   VAPOR   LIQUID   LIQUID   LIQUID   LIQUID   VAPOR   VAPOR   LIQUID   VAPOR   VAPOR   LIQUID   VAPOR   VAPOR                   Substream: MIXED                                                                   Mole Frac       WATER   0   0.1706242   0.1683706   0   0   0   0   0   0   1   0   0   0   0.743   0.01       N2   3.29E−04   1.17E−03   1.17E−03   0   0   0   0   5.00E−03   5.00E−03   0   1   0   0   0   3.00E−03       O2   0   7.05E−11   2.25E−11   0   0   0   0   0.995   0.995   0   0   0   0   0   0       CO2   0   0.0700694   0.0723234   0   0   0   0   0   0   0   0   0   0   0   0.116       CO   0   0.3104558   0.3082029   0   0   0   0   3   0   0   0   0   0   0   0.34       H2   0   0.2112548   0.2139049   0   0   0   0   0   0   0   0   0   0   0   0.33       CL2   0   1.05E−07   5.86E−08   0   0   0   0   0   0   0   0   0   0   0.257   0       CL   0   2.86E−05   1.75E−05   0   0   0   0   3   0   0   0   0   0   0   0       CH4   0   1.35E−03   1.35E−03   0   0   0   0   3   0   0   0   1   0   0   1.00E−03       HCN   0   9.96E−08   9.25E−05   0   0   0   0   0   0   0   0   0   0   0   0       NH3   0   8.11E−07   8.13E−07   0   0   0   0   0   0   0   0   0   0   0   0       FORMHYDE   0   2.89E−07   2.95E−07   0   0   0   0   0   0   0   0   0   0   0   0       BENZENE   1.49E−03   1.53E−07   1.53E−07   0   0   0   0   0   0   0   0   0   0   0   0       SOOT   0   4.50E−03   4.50E−03   0   0   0   0   0   0   0   0   0   0   0   0       FECL3   4.00E−05   3.59E−06   3.9E−06   0   0   0   0   0   0   0   0   0   0   0   0       DOWTH-RP   4.00E−05   3.59E−06   3.89E−06   0   0   0   0   0   0   0   0   0   0   0   0       Mass Flow LB/HR   0   0   0   1   1   1   1   0   0   0   0   0   1   0   0       WATER   0   5115.789   5048.189   0   0   0   0   0   0   1.00E−03   0   0   0   5802.188   1201.463       N2   1.250002   54.3275   54.32505   0   0   0   0   41.92633   41.02633   0   1.00E−03   0   0   0   7937.243       O2   0   3.75E−06   1.20E−06   0   0   0   0   9530.3   9530.3   0   0   0   0   0   0       CO2   0   5132.189   5297.33   0   0   0   0   0   0   0   0   0   0   0   462.1573       CO   0   14472.71   14367.61   0   0   0   0   0   0   0   0   0   0   0   1428.547       H2   0   709.7647   716.3099   0   0   0   0   0   0   0   0   0   0   0   62.82928       HCL   0   13989.56   13990.23   0   0   0   0   0   0   0   0   0   0   4137.012   0       CL2   0   13989.56   13990.23   0   0   0   0   0   0   0   0   0   0   4107.012   0       CL   0   1.085736   1.033508   0   0   0   0   0   0   0   0   0   0   0   0       CH4   0   33.10844   36.10644   0   0   0   0   0   0   0   0   1.00E−00   0   0   1.51507       HCN   0   4.03E−03   4.16E−03   0   0   0   0   0   0   0   0   0   0   0   0       NH3   0   0.0201496   0.0230315   0   0   0   0   0   0   0   0   0   0   0   0       FORMHYDE   0   0.0144203   0.0147523   0   0   0   0   0   0   0   0   0   0   0   0       NAPTHALN   0   0.0158562   0.0158562   0   0   0   0   0   0   0   0   0   0   0   0       BENZENE   16.37100   0.0190582   0.0190582   0   0   0   0   0   0   0   0   0   0   0   0       SOOT   0   90.03299   90.03299   0   0   0   0   0   0   0   0   0   0   0   0       FECL3   1.050234   1.050234   1.050234   0   0   0   0   0   0   0   0   0   0   0   0       DOWTH-RP   0   0   0   5.00E+05   5.00E+05   5.00E+05   5.00E+05   0   0   0   0   0   5   0   0       ACI Components   2003.8033       Total flow LB/   140.6467   1664.297   1664.289   2115.487   2115.767   2115.446   2115.467   299.3297   299.3297   5.55E−05   3.57E−05   6.25E−08   0.0211544   439.4496   94.44552       MOL/HOUR       Total Flow LB/HR   18005.1   39802.32   39802.32   5.00E+05   5.00E+05   5.00E+05   5.00E+05   9572.227   9572.227   1.00E−03   1.00E−03   1.00E−06   5   10000   2000       Total Flow GAL/   35.60107   77079.35   75149.24   1108.471   1108.515   1114.251   1108.471   1897/831   2793.588   2.31E−06   2.27E−04   2.19E−07   9.75E−03   4667.781   334.4008       MIN       Temperature C.   150   1450   1397.446   134.7998   200.0458   205.9968   200   30   150   204.4441   30   30   30   200   195       Pressure PSIG   239   75   74.5   15   50   135   15   100   95   235   100   160.3569   85.30405   90   300       Vapor frac   0   1   1   0   0   0   0   1   1   0   1   1   0   1   1       Enthalpy BTU/HR   0.09E+06   5.12E+07   5.27E+07   6.71E+07   6.71E+07   7.01E+07   6.71E+07   11335.69   4.88E−05   −0.513492   1.54E−03   −2.01E−03   −9.871647   −3.74E+07   −4.18E+00       Density LB/CU FT   63.05406   0.0640565   0.0657017   56.23808   56.23505   55.04578   56.23807   0.6208323   0.4287346   53.90761   0.5485749   3.5086655   63.90579   0.2670977   0.7456641       Average Mwe   128.0186   23.79522   23.79538   236.3569   236.3568   236.3568   236.3568   31.97887   31.97887   10.01526   28.01348   16.04276   236.3568   22.75574   21.17623                    
         [0074]    [0074]                                                                       TABLE 3B                           Stream Number:   210   310                                                                                                                                                                               TO:   0.             0.3310                                                                                                                                                                               From:                                                                                                                                                                                       VA             MIXED   LIQUID   LIQUID   LIQUID   LIQUID   LIQUID   LIQUID   LIQUID   VAPOR                 VAPOR                 LIQUID       Mole Frac       H2O                                                                                                                                                                                                           CH4                                                                                                                                                                                                           CL2                               0                                                                                                                   0                 0       CO2                                                                                                                                                                                                           CO                                                                                                                                                                                                                         0                                                                                                                                                                           0                                                                                                                                                                                                                             BENZENE                                                                                                                                                                                                           H                                                                                                                                                                                                                     HCLO   0                 0                                                                                       0                 0                 0       HCL                                                                                                                                                                                                           HLN                                                                                                                                                                                                           N2                                                                                                                                                                                                                         0                                                                                                                   0                 0                                                                                                                                                                                                                                       0       PY                                                                                                                                                                                                                                                               0   0   0   0   0   0   0                                             0   0                     0   0   0   0   0   0   0   0   0   0   0   0   0   0                     0                                                                                                                   0                 0                                   CL   0                                                                                                                   0                 0                                   O   0                 0                                                                                       0                 0                 0       OH   0                 0                                                                                       0                 0                                                 0                 0                                                                                       0                 0                                   HCO   0                                                                                                                   0                 0                                                 0                                                                                                                   0                 0                                   NH2CO2   0                 0                                                                                       0                 0                                                 0                                                                                                                   0                 0                                             Flow       HCO                                                                                                                                                                                                                                                                                                                                                                                                                                                                           0                                                                                       0                 0                 0       CO2                                                                                                                                                                                                           CO                                                                                                                                                                                                           CYAN   0                                                                                                                                                                           0                                                                                                                                                                                                                             BENZENE                                                                                                                                                                                                           H2                                                                                                                                                                                                           HCLO   0                 0                                                                                       0                 0                 0       HCL                                                                                                                                                                                                           HCN                                                                                                                                                                                                                     N2                                                                                                                                                                                                                     NAPH             0                                                                                                                   0                 0                 0                                                                                                                                                                                                                                                                                                                                                                                                                                                                                             0   0   0   0   0   0   0                                             0   0       PY             0   0   0   0   0   0   0   0   0   0   0   0   0   0       OH   0                                                                                                                   0                 0                                   CL   0                                                                                                                   0                 0                                                 0                 0                                                                                       0                 0                 0                     0                 0                                                                                       0                 0                 0       COO             0                 0                                                                                       0                 0                                   HCO             0                                                                                                                   0                 0                                   H              0                                                                                                                   0                 0                                                 0                 0                                                                                       0                 0                 0                     0                                                                                                                   0                 0                 0                     0   0   0   0   0   0   0   0   0   0   0   0   0   0       Total Flow                                                                                                                                                                                                                      Total Flow                                                                                                                                                                                                                      Total Flow                                                                                                                                                                                                                      Temperature                                                                                                                                                                                                                      Pressure PSI                                                                                                                                                                                                           Vapor                                          0   0   0   0   0   0   0   0                 1   0   0       E                                                                                                                                                                                                                     Density                                                                                                                                                                                                                                                                                                                                                                                                                                                      QUID PHAS                                                                                                                                                                                                                                                                                                                                                                                                                        
         [0075]    [0075]                                                                                                                   TABLE 3C                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                        
         [0076]    [0076]                                           TABLE 3D                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                                        
         [0077]    [0077]                                                                                                                   TABLE 3E