US20030162846A1 - Process and apparatus for the production of synthesis gas - Google Patents

Process and apparatus for the production of synthesis gas Download PDF

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Publication number
US20030162846A1
US20030162846A1 US10/083,778 US8377802A US2003162846A1 US 20030162846 A1 US20030162846 A1 US 20030162846A1 US 8377802 A US8377802 A US 8377802A US 2003162846 A1 US2003162846 A1 US 2003162846A1
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United States
Prior art keywords
syngas product
syngas
produce
mixture
reactive diluent
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Abandoned
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US10/083,778
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English (en)
Inventor
Shoou-l Wang
Shankar Nataraj
John Repasky
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Gtlpetrol Holding Co LLC
NATIONAL INSTITUTE FOR STRATEGIC TECHNOLOGY ACQUISITION AND COMMERCIALZATION
Air Products and Chemicals Inc
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Air Products and Chemicals Inc
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Publication date
Application filed by Air Products and Chemicals Inc filed Critical Air Products and Chemicals Inc
Priority to US10/083,778 priority Critical patent/US20030162846A1/en
Priority to PCT/IB2003/000695 priority patent/WO2003070629A1/fr
Priority to US10/518,038 priority patent/US7670586B2/en
Priority to EP03712473.2A priority patent/EP1492725B1/fr
Priority to CA2482404A priority patent/CA2482404C/fr
Priority to AU2003216567A priority patent/AU2003216567B2/en
Publication of US20030162846A1 publication Critical patent/US20030162846A1/en
Assigned to NATIONAL INSTITUTE FOR STRATEGIC TECHNOLOGY ACQUISITION AND COMMERCIALZATION reassignment NATIONAL INSTITUTE FOR STRATEGIC TECHNOLOGY ACQUISITION AND COMMERCIALZATION CHANGE OF NAME (SEE DOCUMENT FOR DETAILS). Assignors: MID-AMERICA COMMERCIALIZATION CORPORATION
Assigned to AIR PRODUCTS AND CHEMICALS, INC. reassignment AIR PRODUCTS AND CHEMICALS, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: NATARAJ, SHANKAR, REPASKY, JOHN, WANG, SHOOU-I
Assigned to GTLPETROL LLC reassignment GTLPETROL LLC LICENSE (SEE DOCUMENT FOR DETAILS). Assignors: NATIONAL INSTITUTE FOR STRATEGIC TECHNOLOGY ACQUISITION AND COMMERCIALIZATION
Assigned to GTLPETROL LLC reassignment GTLPETROL LLC CORRECTIVE ASSIGNMENT TO CORRECT THE TYPOGRAPHICAL ERROR IN LICENSOR'S NAME IN LICENSE AGREEMENT PREVIOUSLY RECORDED ON REEL 023032 FRAME 0415. ASSIGNOR(S) HEREBY CONFIRMS THE LICENSE AGREEMENT. Assignors: NATIONAL INSTITUTE FOR STRATEGIC TECHNOLOGY ACQUISITION AND COMMERCIALIZATION
Assigned to MID-AMERICA COMMERCIALIZATION CORPORATION reassignment MID-AMERICA COMMERCIALIZATION CORPORATION TECHNOLOGY DONATION AGREEMENT Assignors: AIR PRODUCTS AND CHEMICALS, INC.
Priority to US12/704,311 priority patent/US8383078B2/en
Priority to US13/774,833 priority patent/US9011814B2/en
Priority to US14/691,395 priority patent/US10450195B2/en
Assigned to GTLPETROL HOLDING CO. LLC reassignment GTLPETROL HOLDING CO. LLC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: GTLPETROL LLC
Priority to US16/243,320 priority patent/US20190284047A1/en
Abandoned legal-status Critical Current

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    • C10J2300/0983—Additives
    • C10J2300/0986—Catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/32—Hydrogen storage
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the present invention relates to a process and apparatus for the production of synthesis gas, particularly for but not necessarily limited to, use in the production of hydrocarbon liquid fuels (e.g. using the Fischer-Tropsch (“F-T”) process), methanol (e.g. by catalytic hydrogenation of carbon monoxide), oxo-alcohols and dimethyl ether (“DME”).
  • hydrocarbon liquid fuels e.g. using the Fischer-Tropsch (“F-T”) process
  • methanol e.g. by catalytic hydrogenation of carbon monoxide
  • oxo-alcohols e.g. by catalytic hydrogenation of carbon monoxide
  • DME dimethyl ether
  • Natural gas may be found in remote locations both on- and offshore. It is generally expensive and impractical to transport natural gas from its source to a distant processing plant. One solution is to convert the gas on-site to a valuable and easily transportable product. In this way, the value of the natural gas may be increased.
  • Natural gas may be converted to synthesis gas (or “syngas”) which is a mixture of carbon monoxide and hydrogen.
  • Syngas may be converted to a solid or liquid synthetic fuel (“synfuel”) or converted to methanol, oxo-alcohols or DME.
  • the ratio of hydrogen to carbon monoxide is preferably about 2 to 1.
  • the conversion products have less volume per unit mass (i.e. have a greater density) than the natural gas. Accordingly, it is more economical to transport conversion products than a corresponding amount of natural gas.
  • Syngas may be produced using a heat exchange reforming (“HER”) process.
  • HER heat exchange reforming
  • a conventional two-step HER process may use natural gas as feedstock and employs a primary exothermic (or heat-generating) unit producing syngas, e.g. from natural gas and oxygen, coupled with a secondary endothermic (or heat-requiring) unit that uses at least a portion of the heat generated in the primary unit to produce further syngas, e.g. by a reforming reaction of natural gas and steam.
  • the syngas generated by the HER feeds the primary exothermic unit, while other HERs operate in parallel to the exothermic unit and augment the syngas production therein.
  • SMR Steam-methane reforming
  • ATR Autothermal reforming
  • CPO Catalytic partial oxidation
  • the oxidation reaction in the primary heat-generating unit is exothermic and, thus, the syngas is produced at elevated temperature.
  • POX produces syngas at a temperature of from 1200 to 1400° C.
  • ATR produces syngas at a temperature of from 900 to 1100° C.
  • CPO produces syngas at a temperature of from 1000 to 1100° C.
  • the excess heat generated in these processes may be used to generate steam, for example in waste heat boilers, that can be used in steam turbines to generate power for air separation systems, air compressors and other equipment.
  • the excess heat may be used with additional natural gas and steam in a separate secondary unit to generate further syngas via steam-methane reforming.
  • This process is the basis of the generic two-step HER process.
  • the high temperature syngas from the primary heat-generating unit is usually introduced to the shell-side of a shell and tube style steam-methane reformer.
  • the tubes may contain conventional steam-methane reforming catalyst over which natural gas and steam react endothermically to form syngas.
  • the heat from syngas on the shell-side of the reformer is used to drive the endothermic steam-methane reforming reaction.
  • the syngas stream leaving the tubes can be separately collected and used to feed the primary exothermic syngas generator.
  • the syngas streams leaving the tubes are combined with the syngas on the shell-side to produce syngas having the desired ratio of hydrogen to carbon monoxide at a temperature of from 500 to 600° C.
  • a secondary unit in which reforming takes place over catalyst using heat taken from the primary heat-generating unit is known as a Heat Exchange Reformer.
  • a Heat Exchange Reformer One such example is described in U.S. Pat. No. 4,919,844 (Wang; published on Apr. 24, 1990) and is called an Enhanced Heat Transfer Reformer (or “EHTR”).
  • EHTR Enhanced Heat Transfer Reformer
  • Other existing HER processes are disclosed in WO-A-98/32817 (Halmo et al; published on Jul. 30, 1998), WO-A-00/09441 (Abbot; published on Feb. 24, 2000), WO-A-00/03126 (Fjellhaug et al; published on Jan. 20, 2000) and U.S. Pat. No. 5,362,453 (Marsch; published on Nov. 8, 1994). These disclosures are also incorporated herein by reference.
  • HER process An example of an HER process is disclosed in U.S. Ser. No. 09/965979 (filed on Sep. 27, 2001 and claiming priority from GB0025150.4 filed on Oct. 13, 2000) and this disclosure is incorporated herein by reference.
  • a POX reactor is used in combination with an EHTR.
  • Hydrocarbon fuel gas is reacted with steam and/or oxygen gas in a syngas generation system to produce a syngas product stream.
  • An oxidant gas is compressed to produce a compressed oxidant gas, at least a portion of which is combusted in the presence of combustion fuel gas to produce combustion product gas.
  • the combustion product gas is expanded to produce power and expanded combustion product gas.
  • Heat from the expanded combustion product gas is recovered by using the expanded combustion product gas to heat steam by heat exchange to produce heated steam, at least a portion of which is used to provide at least a portion of any steam requirement for producing the syngas product stream in the syngas generation system. Additionally or alternatively, at least a portion of the oxygen gas is provided using an ASU that is driven by at least a portion of the power generated by the expansion of the combustion product gas.
  • Syngas product feeding conversion processes will unavoidably contain carbon dioxide.
  • this carbon dioxide behaves like an inert. Whilst it can be vented downstream, the carbon and oxygen capture efficiency of the entire gas to liquid (“GTL”) process is lower, which contributes to the greenhouse effect. It is thus desirable to recycle this carbon dioxide to the front-end syngas generator. It is a primary objective of this invention to enable efficient recycle of carbon dioxide and affect its efficient conversion to useful carbon monoxide, while minimizing the amount of such recycle and usage of oxygen feedstock.
  • the POX process can generate syngas with small amounts of solid carbon particles or soot. This soot could foul or erode the heat exchange surfaces in the downstream HER. It is thus another objective of this invention to reduce or eliminate the potential for problems arising for such solid carbon particles.
  • U.S. Pat. No. 4,731,098 (Marsch: published on Mar. 15, 1988) discloses a reformer in which natural gas and steam are reformed to produce syngas. The syngas is then mixed with natural gas and oxygen or air before the mixture leaves the reformer.
  • Hydrocarbon-containing fuel is exothermically reacted with an oxidant gas comprising molecular oxygen in a first reactor to produce an exothermically-generated syngas product.
  • a stream of reactive diluent fluid is combined with a stream of said exothermically-generated syngas product to produce a reactive mixture and the reactive mixture is reacted in a second reactor to produce a reacted syngas product.
  • this reacted syngas may be introduced into the secondary reforming unit in an HER process.
  • One advantage of the invention is that the reacted syngas product is cooled before being introduced into the secondary unit thereby avoiding negatively affecting the mechanical integrity of the secondary unit.
  • the reactive diluent fluid comprises gases produced downstream in the overall process that would otherwise be vented to the atmosphere or that would have to undergo treatment before venting to atmosphere, the level of pollutant emissions to the environment may be reduced and corresponding cost savings may be achievable from the pollutant gas treatment processes.
  • Carbon dioxide and hydrogen present in the reactive mixture may be converted into water and valuable carbon monoxide. This conversion is particularly useful when the reactive diluent fluid is carbon dioxide. However, it still has useful application when the reactive diluent fluid is not carbon dioxide but the source of hydrocarbon fuel (e.g. natural gas) contains significant quantities of carbon dioxide. The additional carbon monoxide produced may be used downstream to improve the yield of the natural gas conversion products. If the reactive diluent fluid comprises carbon dioxide that has been recycled from downstream processes then there is a further advantage in that the level of carbon dioxide emission to the environment is reduced.
  • the reactive diluent fluid comprises carbon dioxide that has been recycled from downstream processes then there is a further advantage in that the level of carbon dioxide emission to the environment is reduced.
  • the gas exiting such a downstream process can contain significant amounts of carbon dioxide.
  • Such gas typically also contains unconverted syngas as well as light hydrocarbons.
  • Such gas can be recycled as diluent without further processing in which case the other components (other than carbon dioxide) would participate in the reaction, increasing the production of desired synfuel.
  • the carbon dioxide content of such gas can be isolated in an acid gas removal (“AGR”) unit for recycle to the front end of the process and the other components could be used as fuel.
  • AGR acid gas removal
  • a reverse water gas shift reaction may be used to convert the carbon dioxide and hydrogen into water and valuable carbon monoxide. Such a reaction is endothermic and, thus, uses heat from the reactive mixture thereby imposing additional cooling on the syngas and assisting in the overall ability to maintain mechanical integrity in the secondary reforming unit of the HER process.
  • Reaction (I) is thermodynamically less favourable than reaction (II) and requires higher temperatures.
  • the temperature at the exit of the HER tubes is necessarily lower than the temperature of the gas from the exothermic reactor. Therefore, the carbon dioxide is not completely converted when the syngas exits the tubes of the reformer unit. If the HER is a parallel type (such as an EHTR), this can lead to excessive costs associated with the recycle of carbon dioxide.
  • carbon dioxide is converted to carbon monoxide in a reverse water gas shift reaction before being fed to the secondary reformer unit.
  • the following reaction takes place in the reverse water gas shift reactor:
  • Reaction (III) is in equilibrium but the position of the equilibrium is pushed far over to the right hand side due to the high temperature of the syngas and the continual introduction of carbon dioxide. Therefore, by recycling carbon dioxide, injecting it into the exothermically-generated syngas product produced in the primary heat-generating unit and subjecting the reactive mixture to a reverse water gas shift reaction, more carbon dioxide may be converted to useful carbon monoxide. This conversion minimizes the size of the carbon dioxide recycle loops and associated costs.
  • the reverse shift reaction zone assists in the gasification of any soot in the syngas from a POX-type exothermic unit, mitigating any erosion or fouling concerns in the surfaces of heat exchangers downstream, including HERs, boilers and preheaters. It can also eliminate the requirement of a scrubber that normally accompanies POX processes.
  • FIG. 1 is a flowsheet describing one embodiment of the process of the present invention.
  • FIG. 2 is a flowsheet describing a hydrocarbon conversion process in which the process of FIG. 1 is integrated with a downstream generic syngas conversion process to produce hydrocarbon liquid fuels or other liquid products.
  • any solid carbon present in the exothermically-generated syngas product can be at least partially gasified mitigating fouling, erosion or plugging of downstream heat exchangers such as HERs, boilers or preheaters.
  • the reactive mixture comprises carbon dioxide
  • at least a portion of the carbon dioxide may be reacted together with at least a portion of the molecular hydrogen in said mixture over a catalyst in a reverse water gas shift reaction zone to produce a carbon monoxide-enriched syngas product.
  • the reactive mixture comprises solid carbon particles
  • at least a portion of the particles may be gasified by reaction with at least one other component of the mixture in a gasification zone to produce a solid carbon-depleted syngas product.
  • the gasification reaction preferably occurs on the surface of a gasification reaction support structure and may be catalysed.
  • the process preferably further comprises endothermically reforming hydrocarbon-containing fuel gas with steam over a catalyst in a heat exchange reformer to produce a heat exchange-reformed syngas product. At least a portion of the heat required in the generation of said heat exchange-reformed syngas product is obtained by recovering heat from said reacted syngas product thereby cooling the reacted syngas product. Use of this heat in this way provides further overall cooling of the syngas.
  • the heat exchange-reformed syngas product may be combined with the reacted syngas product prior to heat recovery.
  • the reactive diluent fluid is a gas
  • the exothermically-generated syngas product is first cooled via sensible heat exchange.
  • the reactive diluent fluid is a liquid
  • inital cooling occurs via vaporisation and sensible heat exchange.
  • the reactive diluent fluid may be recovered and recycled from downstream processing of syngas.
  • the reactive diluent fluid may promote the gasification of any solid carbon particles or soot present in the reactive mixture.
  • the reactive diluent fluid may be imported from an external source.
  • the reactive diluent fluid may comprise carbon dioxide separated, e.g. by acid gas recovery and recycled from downstream syngas or recovered and recycled from downstream processing of syngas. Alternately, the residual gas from a GTL reactor comprising carbon dioxide can be recycled without processing in an AGR unit.
  • the reactive diluent may comprise the products of a combustion process which would contain a significant quantity of carbon dioxide. The combustion products may be selected from the group consisting of combustion furnace flue gases and gas turbine exhaust gas.
  • the reactive diluent fluid may comprise carbon dioxide imported from an external source.
  • the reactive diluent fluid may comprise carbon dioxide and methane either alone or together with other hydrocarbon(s) such as ethane, propane, butane, pentane, hexane and/or their isomers.
  • the diluent may be a residual effluent of the reactor after separation of synfuel and water. In this case, it would comprise of carbon dioxide, unreacted carbon monoxide and molecular hydrogen, low molecular weight paraffins, olefins and oxygenates. The recycling of these gases increases their utilization and increases the overall GTL process efficiency.
  • the reacted syngas product from the reformer is preferably used in a downstream conversion process to produce conversion products selected from the group consisting of hydrocarbon liquid fuels, methanol, DME and oxo-alcohols.
  • apparatus for the production of syngas comprising carbon monoxide and molecular hydrogen comprising:
  • the first reactor is preferably selected from the group consisting of a POX reactor, an ATR or a CPO reactor.
  • the second reactor preferably has a reverse water gas shift reaction zone in which at least a portion of the carbon dioxide and at least portion of the molecular hydrogen in the reactive mixture are reacted together over a catalyst to produce a carbon monoxide-enriched syngas.
  • the second reactor may have a gasification reaction zone in which at least a portion of the solid carbon particles is gasified by reaction with at least one other component of the reactive mixture to produce a solid carbon-depleted syngas.
  • the apparatus preferably further comprises a heat exchange reformer in which hydrocarbon-containing fuel gas is reformed endothermically with steam over a catalyst to produce a heat exchange-reformed syngas product, wherein at least a portion of the heat required in the generation of said heat exchange-reformed syngas product is obtained by recovering heat from said reacted syngas product thereby cooling the reacted syngas product.
  • a heat exchange reformer in which hydrocarbon-containing fuel gas is reformed endothermically with steam over a catalyst to produce a heat exchange-reformed syngas product, wherein at least a portion of the heat required in the generation of said heat exchange-reformed syngas product is obtained by recovering heat from said reacted syngas product thereby cooling the reacted syngas product.
  • the reformer is preferably a shell and tube style reformer in which the endothermic reforming reaction occurs within the tubes and the reacted syngas product is introduced to the shell-side.
  • the reformer is an EHTR.
  • apparatus for the production of syngas comprising carbon monoxide and molecular hydrogen comprising:
  • a reverse water gas shift reaction zone in which carbon dioxide in said mixture is reacted together with molecular hydrogen in said mixture over a catalyst to produce a carbon monoxide-enriched syngas product
  • a gasification reaction zone in which solid carbon particles in said mixture are gasified with at least one other component in said mixture to produce a solid carbon-depleted syngas product.
  • apparatus for the production of syngas comprising carbon monoxide and molecular hydrogen comprising:
  • a heat exchange reformer in which hydrocarbon-containing fuel gas is reformed endothermically with steam over a catalyst to produce a second syngas product and in which at least a portion of said second syngas product is combined with at least a portion of said carbon monoxide-enriched syngas product to produce a combined syngas product, wherein at least a portion of the heat generated in the exothermic reaction producing said first syngas product is used to drive the endothermic reforming reaction.
  • the first reactor is preferably a POX reactor as this reactor produces the highest temperature syngas (when compared with ATR and CPO) and the higher the temperature of the syngas from the primary heat-generating unit, the higher the conversion of carbon dioxide in the reactive diluent and the better the efficiency of downstream HER processing.
  • the POX reactor is preferably used in combination with an EHTR as the heat exchange reformer.
  • a stream 2 of natural gas is preheated by indirect heat exchange 8 , hydrodesulfurized as required, and divided into a first portion 4 and a second portion 6 .
  • the first portion 4 is introduced into a POX reactor 12 .
  • a stream 14 of oxygen is pre-heated by indirect heat exchange 16 and the pre-heated oxygen stream 18 is also fed to the POX reactor 12 .
  • the natural gas and the oxygen are reacted together in the POX reactor 12 to produce first syngas product.
  • a stream 20 of first syngas product is removed from the POX reactor 12 at a temperature of from 1200 to 1400 20 C.
  • a stream 22 comprising carbon dioxide is introduced to and cools the first syngas product stream 20 .
  • the cooled stream 24 is fed to a reverse water gas shift reactor 26 in which at least a portion of the carbon dioxide from the cooled stream 24 is reacted with at least a portion of the hydrogen from the cooled stream 24 to produce carbon monoxide and water.
  • the catalytic reaction is endothermic and, thus, a further cooling effect on the syngas is observed.
  • a stream 28 of carbon monoxide-enriched syngas is removed from the reverse water gas shift reactor 26 and introduced to the shell-side of an EHTR 30 .
  • a stream 32 of steam is introduced to the second portion 6 of the natural gas and the combined stream 34 is pre-heated by indirect heat exchange 36 .
  • the pre-heated combined stream 38 is introduced to the tube-side of the EHTR 30 .
  • the tubes of the EHTR 30 contain conventional steam-methane reforming catalyst and the natural gas and the steam react to form second syngas product. Heat from the shell-side of the EHTR 30 provided at least in part by the carbon monoxide-enriched syngas, is used to drive the endothermic catalytic steam-methane reforming reaction.
  • the second syngas product leaving the tubes of the EHTR 30 is combined with the first syngas product to form a combined syngas product.
  • a stream 40 of combined syngas product is removed for downstream processing, in particular for the synthesis of hydrocarbon liquid fuels (e.g. by the F-T process), methanol (e.g. by the catalytic hydrogenation of carbon monoxide), oxo-alcohols and DME.
  • Table 1 contains data for the composition of various streams in the process of FIG. 1 calculated in a computer simulation. 4 6 22 24 28 38 STREAM ID 2 NG TO NG TO 18 20 FT QUENCH CATBEDO EHTR 40 STREAM NG FEED POX EHTR POX O2 POX OUT OFFGAS ED UT FEED EHTR OUT Temperature F 60 685 685 449.3 2450 100 2269.7 2185.7 950 1094.2 Pressure psia 515 494 494 460 412 600 412 412 484 412 Mole Flow lb mol/hr 18542 14471 4653 9187 43416 2301 45717 45908 14499 68238 Enthalpy MMBtu/hr ⁇ 625.0 ⁇ 371.6 ⁇ 119.5 24.3 ⁇ 348.3 ⁇ 390.9 ⁇ 739.2 ⁇ 739.2 ⁇ 1055.0 ⁇ 1814.0 COMPONENTS Mole Flow lb
  • a syngas generation system 42 of the type depicted in FIG. 1 is fed by a stream 2 of hydrocarbon fuel gas, a stream 14 of oxygen or air and a stream 32 of steam.
  • a stream 40 of syngas is removed from the syngas generation system 42 and fed to a syngas conversion system 44 .
  • the syngas conversion system 44 may use an F-T process to synthesize liquid hydrocarbons or involve the synthesis of methanol, DME or oxo-alcohols.
  • a stream 46 of raw conversion product is removed from the syngas conversion system 44 and upgraded and refined 50 to produce the liquid products 52 .
  • a stream 22 of reactive diluent gas is recycled from the syngas conversion system 44 to the syngas generation system 42 .
  • a recycle stream 54 may also be taken from the product upgrading and refining process 50 .

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US10/083,778 US20030162846A1 (en) 2002-02-25 2002-02-25 Process and apparatus for the production of synthesis gas
AU2003216567A AU2003216567B2 (en) 2002-02-25 2003-02-24 A process and apparatus for the production of synthesis gas
US10/518,038 US7670586B2 (en) 2002-02-25 2003-02-24 Process and apparatus for the production of synthesis gas
EP03712473.2A EP1492725B1 (fr) 2002-02-25 2003-02-24 Procede et appareil de production d'un gaz de synthese
CA2482404A CA2482404C (fr) 2002-02-25 2003-02-24 Procede et appareil de production d'un gaz de synthese
PCT/IB2003/000695 WO2003070629A1 (fr) 2002-02-25 2003-02-24 Procede et appareil de production d'un gaz de synthese
US12/704,311 US8383078B2 (en) 2002-02-25 2010-02-11 Process and apparatus for the production of synthesis gas
US13/774,833 US9011814B2 (en) 2002-02-25 2013-02-22 Process and apparatus for the production of synthesis gas
US14/691,395 US10450195B2 (en) 2002-02-25 2015-04-20 Process and apparatus for the production of synthesis gas
US16/243,320 US20190284047A1 (en) 2002-02-25 2019-01-09 Process and apparatus for the production of synthesis gas

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US13/774,833 Expired - Lifetime US9011814B2 (en) 2002-02-25 2013-02-22 Process and apparatus for the production of synthesis gas
US14/691,395 Expired - Lifetime US10450195B2 (en) 2002-02-25 2015-04-20 Process and apparatus for the production of synthesis gas
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US7670586B2 (en) 2010-03-02
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US10450195B2 (en) 2019-10-22
US20060128818A1 (en) 2006-06-15
US9011814B2 (en) 2015-04-21
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US20190284047A1 (en) 2019-09-19
AU2003216567B2 (en) 2008-06-12
US8383078B2 (en) 2013-02-26
WO2003070629A1 (fr) 2003-08-28
US20100140553A1 (en) 2010-06-10

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