WO2003027062A1 - Installations integrees de fabrication d'uree et procedes relatifs - Google Patents

Installations integrees de fabrication d'uree et procedes relatifs Download PDF

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Publication number
WO2003027062A1
WO2003027062A1 PCT/US2001/030017 US0130017W WO03027062A1 WO 2003027062 A1 WO2003027062 A1 WO 2003027062A1 US 0130017 W US0130017 W US 0130017W WO 03027062 A1 WO03027062 A1 WO 03027062A1
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WIPO (PCT)
Prior art keywords
ammonia
unit
syngas
fischer
urea
Prior art date
Application number
PCT/US2001/030017
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English (en)
Inventor
Mark S. Bohn
Charles B. Benham
Richard O. Sheppard
Dennis L. Yakobson
Original Assignee
Rentech, Inc.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Rentech, Inc. filed Critical Rentech, Inc.
Priority to BR0117144-5A priority Critical patent/BR0117144A/pt
Priority to AU2001296308A priority patent/AU2001296308B2/en
Priority to PCT/US2001/030017 priority patent/WO2003027062A1/fr
Priority to CNB018238246A priority patent/CN100396662C/zh
Priority to CA002461685A priority patent/CA2461685A1/fr
Publication of WO2003027062A1 publication Critical patent/WO2003027062A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • C01B13/0259—Physical processing only by adsorption on solids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C273/00—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups
    • C07C273/02—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds
    • C07C273/10—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds combined with the synthesis of ammonia
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used
    • C10G2/331—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals
    • C10G2/332—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals of the iron-group
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
    • F25J3/04545—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels for the gasification of solid or heavy liquid fuels, e.g. integrated gasification combined cycle [IGCC]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • F25J3/04587—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for the NH3 synthesis, e.g. for adjusting the H2/N2 ratio
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415—Purification by absorption in liquids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/048—Composition of the impurity the impurity being an organic compound
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
    • C—CHEMISTRY; METALLURGY
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling
    • C01B2203/0877—Methods of cooling by direct injection of fluid
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
    • C01B2203/84—Energy production
    • C—CHEMISTRY; METALLURGY
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0043—Impurity removed
    • C01B2210/0046—Nitrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
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    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
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    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1643—Conversion of synthesis gas to energy
    • C10J2300/165—Conversion of synthesis gas to energy integrated with a gas turbine or gas motor
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1659—Conversion of synthesis gas to chemicals to liquid hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1668—Conversion of synthesis gas to chemicals to urea; to ammonia
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
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    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
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    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • C10J2300/1675—Integration of gasification processes with another plant or parts within the plant with the production of electricity making use of a steam turbine
    • C—CHEMISTRY; METALLURGY
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    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
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    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1678—Integration of gasification processes with another plant or parts within the plant with air separation
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    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen
    • 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
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • 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
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • Syngas generators such as reformers and gasifiers of hydrocarbon fluids and solid carbonaceous materials and Fischer Tropsch (FT) units for primarily for creating liquid hydrocarbons from syngas are combined to create an integrated plant for providing one or more of urea, ammonia, carbon dioxide, electric power, and even sulfur when dealing with sulfur-containing raw material.
  • FT Fischer Tropsch
  • the integrated plants and processes of this invention can help reduce the amount of C0 2 currently vented into the air through the production of the various products later discussed in the description of the manufacturing plant flow diagrams. Further, the plants of this invention produce substantial energy savings by balancing exothermic and endothermic reactors as discussed below.
  • the multi-product plants of this invention provide a mechanism for packaging the various unit processes required for the utilization of this invention in a manner that the resulting plants can be utilized to supply electricity for a platform, eliminate the need for flares, convert the waste gases and liquids normally flared into liquid hydrocarbons, ammonia and/or urea while substantially eliminating local CO 2 emissions.
  • Solid commercial products can also be produced for agriculture, e.g., sulfur and urea prills.
  • Such self-contained plants provide trade-offs; for offshore petroleum and/or natural gas platforms, which can improve their economic life span. This is particularly true where the deposits being recovered are sour or include some CO 2 production.
  • Ammonia, carbon dioxide, hydrocarbons, electric power and urea are producible as products by the reaction of oxygen, water and a carbon source in a syngas generator to produce a syngas, utilizing a water gas shift mechanism to provide CO 2 , reacting the syngas in an FT reactor to produce FT hydrocarbons and hydrogen, reacting the hydrogen with nitrogen from the air separation oxygen plant to form ammonia, then reacting the CO 2 and ammonia to form urea.
  • Electric power can be produced by combustion of hydrogen in a gas turbine used to drive an electricity generator and/or utilizing steam formed during syngas production to drive a steam turbine which, in turn, drives an electricity generator. Sulfur and various heavy metals can be recovered when sulfur or metal- containing carbon sources are utilized. As noted, a number of the compounds, an element and electric power produced in the manufacture of ammonia can be "packaged" for commercial sale.
  • Figure 1 depicts a syngas producing unit and an FT unit combined to provide liquid hydrocarbons and electric power.
  • Figure 2a utilizes the basic plan of Figure 1 and delineates the minimal equipment and indicates the valving and other plumbing changes needed to convert the unit of Figure 1 into an ammonia manufacturing plant utilizing hydrocarbon gases from a substantially solid carbonaceous feed such as coal and petroleum refining residues.
  • Figure 2b depicts the added equipment needed to convert the ammonia produced in the plant of Figure 2a into a urea plant.
  • Figure 3a and 3b teach an alternate exemplary plant layout for manufacturing urea utilizing natural gas as the syngas feedstock.
  • crushed coal, water (H 2 O), preferably as steam, and oxygen (O 2 ) are introduced into the syngas generator 11 through piping 12, 13 and 14, respectively.
  • the oxygen is preferably from a cryogenic air separation unit 15.
  • pressure swing absorption can also be utilized. Either can provide nitrogen (N 2 ) for an ammonia cNH3-)— lant -(not -shownyV
  • the hot- gases are- exhausted- from, the syngas generator 11 at temperatures of 2400°F to 2700 °F and are cooled in one or more water-cooled quench units 16 to remove slag and other minerals.
  • the cooled syngas and soluble impurities are piped into a heat recovery steam generator (HRSG) 17 which is used to heat the feed water (FW) to steam of a desired temperature, e.g., 230°F to 600°F, and provide steam to power steam turbine 18; the acid gas removal unit (AGR) 19 and the sulfur removal unit (SRU) 20.
  • HRSG heat recovery steam generator
  • the syngas is piped to the acid gas removal unit (AGR) 19 to remove bulk sulfur from the syngas generator 11 output.
  • the resulting gas is then passed through sulfur removal unit (SRU) 20 to remove trace quantities of sulfur.
  • the SRU 20 uses a zinc oxide-based catalyst and is run at temperatures of 600°F to 725°F. with a linear velocity of 4-10 ft/sec.
  • the gaseous treated stream from the SRU is then piped to the FT reactor and product separation unit 21 to obtain the liquid FT hydrocarbon products.
  • the FT reactor and product separator 21 tail gas is piped to remove carbon dioxide via C0 2 removal unit 22.
  • a second portion of the desulfurized syngas is piped to a water gas shift reactor 23, preferably designed for use with a high temperature iron/chrome catalyst.
  • the tail gas stream from the FT reactor and product separation unit 21 is combined with the output of the shift reactor 23 and passed through C0 2 removal unit(s) 22.
  • Combustible components from the C0 2 removal unit(s) 22 are fed to the gas turbine 24 which is used to drive a coupled electricity generator 25.
  • the steam turbine 18 can be used to drive the electrical generator(s) 25.
  • the stack gases of the gas turbine 24 are returned to heat recovery steam generator (HRSG) 17.
  • HRSG heat recovery steam generator
  • the C0 2 absorbed in the C0 2 removal unit 22 is desorbed in the CO 2
  • the equipment differs from that of Figure 1 only to the extent that the non-C0 2 output of the CO 2 removal unit 22 is passed through a hydrogen (H 2 ) removal unit 28 and the recovered hydrogen is piped to an ammonia converter 38 (Fig. 2b).
  • the non- H 2 output of the H 2 removal unit (HRU) 28 is piped to the gas turbine 24 as fuel.
  • the H 2 removal unit 28 utilizes a membrane separator. Such units are manufactured by Monsanto Company, located at St. Louis, Missouri, USA or Air Liquide located at Paris, France.
  • Hydrogen (H 2 ) from the hydrogen removal unit 28 (Fig. 2a) is passed through hydrogen compressor 32 and combined with nitrogen (N 2 ) from air separation unit 15 (See Fig. 1) and the mixture is passed to heater 33 to raise the temperature to about 500°F and introduced into methanator 34 which operates at 500 °F to 600°F utilizing, preferably, a 27-35% nickel oxide catalyst.
  • the methanator utilizes a catalyst which is delivered as nickel oxide on alumina and reduced to nickel on site for operation. A variety of suppliers market the catalyst.
  • the methanator operates at temperatures between about 500°F to 550°F at the inlet and pressures between about 275 to about 375 psig.
  • the methanator 34 product stream is passed through cooler 35 into ammonia/syngas compressor 36.
  • the compressed product stream is cooled in exchanger 37 and is fed to NH 3 converter 38.
  • the resulting ammonia stream returns to the heat exchanger 37 through line 39.
  • the cooled effluent is further cooled in exchanger 41 and still further cooled with a cold stream from ammonia refrigeration unit 42 before passing to separator 43.
  • the condensed ammonia from ammonia separator 43 is then passed through pump 44, piped into a urea synthesizer 29, dried for prilling or made into aqueous solutions of desired concentrations.
  • the liquid oxygen (O 2 ) from air separation unit 40 is passed through cryogenic pump 45, heater 46 and introduced into mixing zone 47.
  • the natural gas is compressed to about 200 to about 500 psia in compressor 48, heated in exchanger 49 and run through a sulfur removal unit 51 to "sweeten” the raw gas and then into another heater 52 before entering the mixing zone 47.
  • the natural gas and oxygen are converted into syngas in syngas generator 53 and cooled in exchanger 54 prior to treatment in CO 2 removal unit 55.
  • the absorbed C0 2 is stripped in stripper 56 prior to recycling to the urea synthesizer 29 (Fig. 3b).
  • the syngas stream passes through heater 57 before entering FT reactor 58.
  • the resulting products are introduced into product separator 59 to provide a liquid hydrocarbon stream with pentane or greater fractions, a stream of aqueous oxygenated hydrocarbons which is pumped from about 200 to about 500 psia by pump 60, and reheated in heat exchangers 61 and 52 prior to entering mixing zone 47.
  • a tail gas stream also flows to mixing zone 47 via compressor 62 while the C0 2 is sent to a CO 2 compressor 63 (Fig. 3b).
  • the flow diagram of Figure 3b shows CO 2 from the C0 2 stripper 56 passing through compressor 63 into urea synthesizer 64 and thence through a urea purification unit 65.
  • the FT tail gas stream then passes a pressure swing absorber 66 to remove H 2 .
  • a hydrogen-lean fraction is used as fuel while the remainder is mixed with nitrogen (N 2 ) from air separation unit 40, piped to heater 67 and thence to methanator 68 which removes the remaining traces of carbon oxides.
  • the product stream from the methanator is piped into cooler 69 and then into ammonia syngas compressor 71.
  • the compressor 71 product is cooled in exchanger 72 and introduced into ammonia converter 73.
  • the ammonia from the converter 73 is fed to the exchanger 72, cooled in exchanger 74 by ammonia refrigeration unit 75.
  • the ammonia stream from exchanger 74 passes through ammonia separator 76.
  • a portion of the effluent from separator 76 is recycled to the ammonia syngas compressor 71 and the remainder is used as fuel.
  • the purified ammonia is passed through pump 77 and mixed with compressed CO 2 before introduction to urea synthesizer 64.
  • the urea produced is then passed through purifier 65 and readied for use or sale.
  • Example 1 is a computer simulation based on the flow sheet of Figure 1.
  • 5500 tpd Pittsburgh #8 coal is gasified with 3328 tpd water and 5156 tpd oxygen. The coal is 74.16% carbon.
  • a portion of the syngas is sent to an FT reactor.
  • the remainder of the syngas is shifted to convert as much of the CO to CO 2 as is possible.
  • This shifted stream is combined with the FT reactor tail gas.
  • C0 is removed from the combined stream and compressed for commercial usage or sequestration.
  • the CO 2 -free gas is sent to the gas turbine to produce power.
  • the flow sheet takes advantage of the water-gas shift activity of an iron- based FT catalyst in converting much of the carbon in the feed coal to CO 2 .
  • This catalyst is discussed in U.S. Patent 5,504,118 issued to Charles B. Benham et al.
  • a computer simulation utilizing the equipment of this flow sheet of 5500 ton per day of coal produces 6000 barrels per day of FT liquids, 400 MW net electrical power, and 10515 ton per day of sequesterable CO 2 . Only 9% of the feed carbon is in the stack gas.
  • Example 2 Coal Gasification to FT Liquids. Electrical Power and Urea.
  • Example 2 is based on the flow sheet of Figures 2a and 2b. This flow sheet builds on the flow sheet of Example 1 by reacting the sequestered CO 2 with ammonia to produce urea. To make the required ammonia, nitrogen from the air separation unit is reacted with hydrogen removed from the gas stream prior to power generation. This demonstrates the synergies possible with the iron-based FT catalyst.
  • This example is based on figures 3a and 3b and the use of a sour natural gas.
  • the natural gas is reformed with oxygen in an autothermal reformer. After cooling the syngas, CO 2 is removed and sent to the urea plant. The syngas is then sent to an FT reactor. Most of the FT tail gas is recycled to the autothermal reactor. The rest is used in the ammonia plant. Ammonia and C0 2 are removed from the syngas and piped to the urea plant.
  • Feedstocks include both natural gas and low value industrial materials, e.g., coal and refinery bottoms having a hydrogen to carbon atom ratio of about 1. Feedstocks can, however, have higher ratios, e.g., natural gas with a ratio approaching 4:1. Many of these materials will include contaminants which must be removed, e.g., sulfur, arsenic and silicaceous materials which are removed during the course of the syngas manufacturing steps as slag or sulfur compounds.
  • the syngas produced can be contaminated with carbon dioxide and unwanted impurities such as chlorine, chlorides and other toxic materials which must be safely removed and stored.
  • iron-based FT catalysts are preferred because they produce CO 2 via their water gas shift activity.
  • the reactors, materials of construction and processes are well known to those skilled in the refining and Fischer Tropsch utilizing industries.
  • the assembly of the reactors taught form the basis of the claimed chemical processing units sequenced in the invention.
  • the sequenced chemical processes, catalysts, temperatures, concentrations and other stated parameters form the basis of the chemical process claims. It is to be understood that the order of the chemical processing units and the process steps and conditions described in Figures and the discussion thereof can be varied and the variations are intended to fall within the claims as taught in the description and Figures.

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Abstract

L'invention concerne une installation destinée à la fabrication d'urée à partir de matériaux carbonés et d'oxygène à partir d'une unité de séparation d'air et d'eau, de préférence de la vapeur, et étant constituée d'une unité de génération de gaz de synthèse, d'une unité de séparation d'air, d'une unité Fischer-Tropsch, d'une unité d'élimination de CO2, d'une unité d'élimination d'hydrogène, d'une unité de méthanation, d'une unité de convertisseur d'ammoniaque et d'une unité de synthèse d'urée. Chaque liquide Fischer-Tropsch, l'ammoniaque, l'hydrogène et l'urée peut être récupéré dans des conditions économiques acceptables. De l'énergie électrique peut être récupérée par ajout d'au moins une turbine à vapeur et une turbine à gaz couplée à un générateur électrique.
PCT/US2001/030017 2001-09-25 2001-09-25 Installations integrees de fabrication d'uree et procedes relatifs WO2003027062A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
BR0117144-5A BR0117144A (pt) 2001-09-25 2001-09-25 Instalações e processos de fabricação de uréia integrados
AU2001296308A AU2001296308B2 (en) 2001-09-25 2001-09-25 Integrated urea manufacturing plants and processes
PCT/US2001/030017 WO2003027062A1 (fr) 2001-09-25 2001-09-25 Installations integrees de fabrication d'uree et procedes relatifs
CNB018238246A CN100396662C (zh) 2001-09-25 2001-09-25 一体化的尿素制造设备和方法
CA002461685A CA2461685A1 (fr) 2001-09-25 2001-09-25 Installations integrees de fabrication d'uree et procedes relatifs

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WO2005005576A1 (fr) * 2003-07-01 2005-01-20 Rentech, Inc. Usine integree de production de liquides obtenus par le procede fischer-tropsch et d'electricite a faibles emissions de co2
US7669403B2 (en) 2004-09-29 2010-03-02 Alstom Technology Ltd. Power plant and operating method
EP2197984A1 (fr) * 2007-09-14 2010-06-23 Rentech, Inc. Intégration d'une centrale à cycle combiné à gazéification intégrée et installation de conversion du charbon en liquide
CN103557675A (zh) * 2013-10-30 2014-02-05 河南开元空分集团有限公司 合成氨化工尾气的深冷精馏液化系统及方法
EP2464600A4 (fr) * 2009-08-12 2015-08-05 4A Technologies Llc Système modulaire et procédé pour la production d'urée à l'aide de gaz naturel délaissé
WO2015173360A1 (fr) * 2014-05-13 2015-11-19 CCP Technology GmbH Procédé et dispositif pour la fabrication d'hydrocarbures synthétiques
EP2867484A4 (fr) * 2012-06-27 2016-03-16 Grannus Llc Production par génération multiple d'énergie et d'engrais au moyen d'une capture d'émissions
WO2016156850A1 (fr) * 2015-04-01 2016-10-06 Compactgtl Plc Traitement d'un gaz d'alimentation contenant du méthane
WO2017096337A1 (fr) * 2015-12-04 2017-06-08 Grannus, Llc Production d'hydrogène par polygénération destiné à être utilisé dans divers procédés industriels
WO2019052877A1 (fr) * 2017-09-13 2019-03-21 Christian Blank Système et procédé pour stocker de l'hydrogène récupéré à partir de charbon

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WO2007115435A1 (fr) * 2006-04-12 2007-10-18 Zte Corporation Procédé de détection automatique de topologie d'entité de contrôle dans le réseau optique commuté automatique
CN100427443C (zh) * 2006-10-11 2008-10-22 太原理工天成科技股份有限公司 一种同时生产甲醇、尿素和人工燃气的方法
CN101434869A (zh) * 2007-11-16 2009-05-20 亚申科技研发中心（上海）有限公司 整合型煤液化方法
WO2010021011A1 (fr) * 2008-08-20 2010-02-25 株式会社Ihi Appareillage de gazéification de combustible
CN101875863B (zh) * 2009-04-29 2013-08-07 四川大学 余热推动循环载热的煤气甲烷化技术与装置
CN104844480B (zh) * 2015-05-20 2017-01-18 中国华能集团清洁能源技术研究院有限公司 一种含氧含氮煤层气合成尿素的系统和方法
CN109595878B (zh) * 2018-12-10 2021-02-09 内蒙古博大实地化学有限公司 一种合成氨、尿素联产液体二氧化碳的方法
CN112121804A (zh) * 2020-10-19 2020-12-25 宁夏大学 一种co加氢铁基催化剂及其制备方法

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Publication number Priority date Publication date Assignee Title
WO2005005576A1 (fr) * 2003-07-01 2005-01-20 Rentech, Inc. Usine integree de production de liquides obtenus par le procede fischer-tropsch et d'electricite a faibles emissions de co2
US7669403B2 (en) 2004-09-29 2010-03-02 Alstom Technology Ltd. Power plant and operating method
US8006478B2 (en) 2004-09-29 2011-08-30 Alstom Technology Ltd. Power plant and operating method
EP2197984A1 (fr) * 2007-09-14 2010-06-23 Rentech, Inc. Intégration d'une centrale à cycle combiné à gazéification intégrée et installation de conversion du charbon en liquide
EP2197984A4 (fr) * 2007-09-14 2012-10-03 Rentech Inc Intégration d'une centrale à cycle combiné à gazéification intégrée et installation de conversion du charbon en liquide
US9617206B2 (en) 2009-08-12 2017-04-11 4A Technologies, Llc Modularized system and method for urea production using stranded natural gas
EP2464600A4 (fr) * 2009-08-12 2015-08-05 4A Technologies Llc Système modulaire et procédé pour la production d'urée à l'aide de gaz naturel délaissé
US9458024B2 (en) 2012-06-27 2016-10-04 Grannus Llc Polygeneration production of power and fertilizer through emissions capture
US10228131B2 (en) 2012-06-27 2019-03-12 Grannus Llc Polygeneration production of power and fertilizer through emissions capture
EP2867484A4 (fr) * 2012-06-27 2016-03-16 Grannus Llc Production par génération multiple d'énergie et d'engrais au moyen d'une capture d'émissions
CN103557675A (zh) * 2013-10-30 2014-02-05 河南开元空分集团有限公司 合成氨化工尾气的深冷精馏液化系统及方法
CN103557675B (zh) * 2013-10-30 2015-05-27 河南开元空分集团有限公司 合成氨化工尾气的深冷精馏液化系统及方法
WO2015173360A1 (fr) * 2014-05-13 2015-11-19 CCP Technology GmbH Procédé et dispositif pour la fabrication d'hydrocarbures synthétiques
WO2016156850A1 (fr) * 2015-04-01 2016-10-06 Compactgtl Plc Traitement d'un gaz d'alimentation contenant du méthane
WO2017096337A1 (fr) * 2015-12-04 2017-06-08 Grannus, Llc Production d'hydrogène par polygénération destiné à être utilisé dans divers procédés industriels
US9957161B2 (en) 2015-12-04 2018-05-01 Grannus, Llc Polygeneration production of hydrogen for use in various industrial processes
US20180222752A1 (en) * 2015-12-04 2018-08-09 Grannus Llc Polygeneration production of hydrogen for use in various industrial processes
US10611634B2 (en) 2015-12-04 2020-04-07 Grannus, Llc Polygeneration production of hydrogen for use in various industrial processes
WO2019052877A1 (fr) * 2017-09-13 2019-03-21 Christian Blank Système et procédé pour stocker de l'hydrogène récupéré à partir de charbon

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CA2461685A1 (fr) 2003-04-03
CN100396662C (zh) 2008-06-25

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