WO1997039235A1 - Integration a synergie d'une unite d'elimination par procede physique des gaz acides de solvants dans des centrales ayant recours a la gazeification - Google Patents

Integration a synergie d'une unite d'elimination par procede physique des gaz acides de solvants dans des centrales ayant recours a la gazeification Download PDF

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Publication number
WO1997039235A1
WO1997039235A1 PCT/US1997/005715 US9705715W WO9739235A1 WO 1997039235 A1 WO1997039235 A1 WO 1997039235A1 US 9705715 W US9705715 W US 9705715W WO 9739235 A1 WO9739235 A1 WO 9739235A1
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Prior art keywords
unit
gas
turboexpander
fuel gas
ofthe
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PCT/US1997/005715
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English (en)
Inventor
Ashok Rao
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Fluor Corporation
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Publication date
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Priority to AU24440/97A priority Critical patent/AU2444097A/en
Publication of WO1997039235A1 publication Critical patent/WO1997039235A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
    • F02B43/00—Engines characterised by operating on gaseous fuels; Plants including such engines
    • 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
    • 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
    • F25J3/04575—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for a gas expansion plant, e.g. dilution of the combustion gas in a gas turbine
    • 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
    • F25J3/04593—The air gas consuming unit is also fed by an air stream
    • 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
    • F25J3/04593—The air gas consuming unit is also fed by an air stream
    • F25J3/04606—Partially integrated air feed compression, i.e. independent MAC for the air fractionation unit plus additional air feed from the air gas consuming unit
    • 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
    • F25J3/04612—Heat exchange integration with process streams, e.g. from the air gas consuming unit
    • 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
    • F25J3/04612—Heat exchange integration with process streams, e.g. from the air gas consuming unit
    • F25J3/04618—Heat exchange integration with process streams, e.g. from the air gas consuming unit for cooling an air stream fed to the air fractionation unit
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/42—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery
    • F25J2260/44—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery using nitrogen for cooling purposes
    • 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]
    • Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
    • 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
    • Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
    • Y02T10/00—Road transport of goods or passengers
    • Y02T10/10—Internal combustion engine [ICE] based vehicles
    • Y02T10/30—Use of alternative fuels, e.g. biofuels

Definitions

  • the present invention relates to integrated gasification power generation plants.
  • Coal gasification plants offer numerous benefits relative to plants which utilize direct combustion of coal.
  • Two promising technologies which integrate coal-gasification with power production include the Integrated Coal Gasification Combined Cycle (IGCC) design and the Integrated Coal Gasification Fuel Cell (IGFC) design.
  • IGCC Integrated Coal Gasification Combined Cycle
  • IGFC Integrated Coal Gasification Fuel Cell
  • fuel gas is produced by partial oxidation of coal, and the fuel gas is then cleaned through reduction of particulates and sulphur containing compounds.
  • the cleaned fuel gas is then combusted in a combustion turbine to generate electric power
  • a typical IGFC plant the cleaned fuel gas is oxidized in the fuel cell to generate the electric power.
  • the term IGCC shall be used generically hereinafter to include all manner of gasification power plants, including both IGCC and IGFC plants, and plants which gasify fuels other than coal.
  • IGCC plants Three important objectives in designing IGCC plants are (1) minimization of pollution; (2) maximization of plant reliability and (3) maximization of energy production relative to capital and fuel costs.
  • H 2 S hydrogen sulfide
  • SO 2 sulfur sulfide
  • both H : S and SO 2 are considered pollutants, and their release into the atmosphere is often restricted by regulation. Since H 2 S in a gasifier effluent typically reaches several thousand parts per million (ppm), and may reach levels of 10,000 to 30.000 ppm or more, some method of desulphurization must be used.
  • IGCC designs have been proposed in which high pressure gasification is combined with direct contact cooling (water quenching) ofthe raw gasifier effluent, and a hot gas turboexpander (which may also be referred to herein simply as an expander) to develop additional power by expanding the gas upstream ofthe combustion turbine.
  • a hot gas turboexpander which may also be referred to herein simply as an expander
  • Such systems can be broadly classified into two categories, (A) those in which the turboexpander is positioned upstream ofthe AGR (the so-called Texaco design of Anand, Jahnke and Olson.
  • a sulphur containing fluid is desulphurized in a desulphurization unit to produce a clean gas.
  • the clean gas is power producingly expanded in an expander to provide refiigeration to the desulpherization unit, and there is at least one intervening process unit other than a heat exchanger with the sulphur containing fluid functionally positioned between the desulphurization unit and the expander.
  • the intervening process unit comprises a membrane separator, synthesis unit or other device involved in coproduction.
  • the intervening process unit comprises a heat exchanger with cold nitrogen expanded downstream of an elevated pressure air separation unit.
  • Figure 1 is a simplified block flow diagram of an IGCC plant according to the present invention.
  • Figure 2 is a simplified block flow diagram of an alternative IGCC plant according to the present invention having a two-stage turboexpander.
  • Figure 3 is a simplified block flow diagram of an alternative IGCC plant according to the present invention having an air separation unit.
  • Figure 4 is a simplified block flow diagram of an IGCC plant according to the present invention.
  • Figure 5 is a simplified block flow diagram of an alternative IGCC plant according to the present invention having a two-stage turboexpander.
  • Figure 6 is a simplified block flow diagram of an alternative IGCC plant according to the present invention having an air separation unit.
  • Figure 1 generally depicts an IGCC plant 1 comprising a feed line 10 containing high pressure raw scrubbed fuel gas, a low temperature gas cooling unit 20, an acid gas removal unit 30, intervening drying unit 40, a turboexpander 50 with associated electrical generator 55, a solvent chiller 60, a humidification/ preheating unit 70, and a combustion turbine 80.
  • Line 10 contains raw scrubbed fuel gas from a gasifier unit (not shown).
  • the gasifier gasifies coal, coke or oil, but in alternative embodiments it may gasify other substances.
  • Many different gasifiers could be utilized, including Texaco, Shell and Noell.
  • the fuel gas in line 10 preferably has a pressure of about 900 - 1200 PSIA, in the case of an IGCC and a temperature of about 300 to 500 °F.
  • Low temperature gas cooling unit 20 cools the high pressure gas from line 10 to about
  • Preferred gas cooling units include a series of heat exchangers.
  • Line 22 carries the cooled high pressure fuel gas from the gas cooling unit 20 to a cold-type, solvent based acid gas removal unit (AGR) 30.
  • AGRs remove at least 98% ofthe sulphur from the fuel gas, and include those utilizing Selexol, Rectesol or Purisol solvents because these utilize a refrigerated physical solvent.
  • preferred AGR units include absorber(s) and stripper(s). Sulphur is preferably recovered from the acid gas produced in the AGR using a sulphur recovery unit (not shown), thereby regenerating the solvent.
  • Line 32 carries the high pressure sweet fuel gas from the AGR 30 to the drying unit 40 when required, where humidity is reduced to a dew point temperature which is lower than the exhaust temperature ofthe turboexpander.
  • Preferred drying units include molecular sieves.
  • Dried fuel gas leaving the drying unit 40 preferably has a pressure of about 800 to 1100 PSIA. and is carried to the turboexpander via line 42.
  • the dried fuel gas is then expanded in turboexpander 50. which produces usable power by driving generator 55. Rather than producing electricity, generator 55 could, for example, be replaced with a compressor.
  • the fuel gas in line 52 would preferably have a temperature of less than 0°F.
  • Lines 34 and 36 carry solvent between the AGR unit 30 and the chiller 60.
  • heat from the solvent in line 36 is transferred to the fuel gas from line 52, increasing the temperature ofthe fuel gas to about 60 °F.
  • the temperature ofthe solvent is reduced from about 90°F to about 25 °F in the case of Selexol.
  • Line 54 carries fuel gas from the chiller 60 to the humidification/preheating unit 70.
  • This unit is optional, and may perform either or both of humidification and preheating functions.
  • Preferred units include a countercurrent packed column and a heat exchanger.
  • Line 72 carries the fuel gas from the humidification/ preheating unit 70 to the combustion turbine 80 where it is combusted, and the combustion products are expanded to produce usable work.
  • the fuel gas may be shghtly preheated before entering the expander such that the gas leaving the chiller does not remain at very low temperatures. This allows optimizing the power developed by the expander and the amount of refrigeration developed.
  • FIG. 2 shows an alternative IGCC design in which the single stage turboexpander 50 of figure 1 has been replaced by a two-stage turboexpander having first stage turboexpander 150A and second stage turboexpander 150B.
  • high pressure scrubbed raw fuel gas would still be produced by a gasifier (not shown), the scrubbed raw fuel gas would enter a low temperature gas cooling unit 120 through line 110, be transferred to an AGR unit 130 via line 122, and then be transferred to an intervening drying unit 140 (when required) via line 132.
  • the fuel gas would then be expanded in the first stage turboexpander 140A, and then transferred to a first solvent chiller 160A.
  • first chiller 160A the fuel gas would undergo heat exchange with solvent flowing through lines
  • an another alternative IGCC plant generally comprises a gasifier unit (not shown), an elevated pressure air separation unit (EP ASU) 211, a physical solvent acid gas removal unit 230, a saturator 270 and a combustion turbine 280.
  • Air separation unit 21 1 produces predominantly oxygen (O 2 ) and nitrogen (N 2 ) streams.
  • the oxygen stream is carried to the gasifier unit (not shown) via line 212.
  • the nitrogen stream is carried along line 214, with a portion ofthe nitrogen being compressed by compressor 215, and then fed into the combustion turbine 280 via line 216.
  • the remainder of the nitrogen is expanded in the nitrogen expander 250, run through a heat exchanger 250, and then either vented to the atmosphere or drawn into the air inlet 282 ofthe combustion turbine 284
  • Raw scrubbed gas from the gasifier unit enters the AGR unit 230 along line 210.
  • the AGR solvent is carried along lines 234 and 236 to the heat exchanger, where it is cooled by heat exchange against the expanded nitrogen. Sulphur removal is provided along line 238.
  • the cleaned (desulphurized) fuel gas is then carried along line 232 to humidifier (saturator) 270, if so desired, where it picks up humidity. Circulating water for the saturation step is carried by line 271A and 271B. Following humidification, the fuel gas is then carried along line 272 to heat exchanger 275 where it is preheated with boiler feed water or other means, and finally carried to the combustor 281 ofthe combustion turbine 280.
  • humidifier saturatedator
  • Combusted gases are expanded by turbine 280 to produce electrical power using power using generator 290.
  • a portion ofthe air compressed by compressor 282 can be shunted via line 217 through one or more heat exchangers such as heat exchanger 218A and 218B. and then carried to the air separation unit 211 via line 219.
  • FIG. 3 has many similarities to the embodiments of figures 1 and 2.
  • a working fluid is expanded to a low temperature, and then reheated using heat from the hot solvent ofthe AGR
  • a working fluid already present in the system such as the fuel gas or the nitrogen from an air separation unit
  • a separate refrigeration unit is obviated and increased efficiency and/or reduced capital costs can be realized.
  • the embodiment of Figure 4 is similar to the embodiment of Figure 1 except that the intervening process unit comprises a membrane separator.
  • raw syn gas (used herein interchangeably with fuel gas) enters a desulphurization unit 330 through line 310, and cleaned syn gas would then pass along line 332 to membrane separator 390.
  • Separator 390 could be used to separate out many different compounds, but here membrane separator is used to separate out a low purity H 2 stream.
  • the H 2 stream then proceeds along line 391 to a pressure swing adsorbtion unit 392, which further separates out H 2 from remaining fuel gas.
  • Clean syn gas which was not separated out in the membrane separator 390 passes along line 392 to turboexpander 350 which provides shaft power to generator 355.
  • the turboexpander 350 reduces the temperature ofthe fuel gas, which then proceeds along line 354 to solvent chiller (heat exchanger) 360 which cools solvent a ⁇ iving from the acid gas removal unit 330 along line 336. Cooled solvent then passes back to the acid gas removal unit 330 along line 334.
  • Fuel gas heated up in solvent chiller 360 then passes along line 362 to humidification and preheating units collectively designated 370, and thence along line 372 to a gas turbine or fuel cell.
  • raw syn gas enters a desulphurization unit 430 through line 410. and cleaned syn gas would then pass along line 332 to synthesis unit 495.
  • Synthesis unit 495 can be used to synthesize many different co-products, and can advantageously be used to synthesize hydrocarbons, including oxygen containing hydrocarbons such as methanol.
  • Unconverted clean syn gas passes along line 492 to turboexpander 450 which provides shaft power to generator 455.
  • the turboexpander 450 reduces the temperature ofthe fuel gas, which then proceeds along line 454 to solvent chiller (heat exchanger) 460 which cools solvent arriving from the acid gas removal unit 430 along line 436.
  • Cooled solvent then passes back to the acid gas removal unit 430 along line 434, and fuel gas heated up in solvent chiller 460 passes along line 462 to humidification and preheating units collectively designated 470, and thence along line 472 to a gas turbine or fuel cell.
  • raw syn gas enters a desulphurization unit 630 through line 610, and cleaned syn gas passes along line 632 to first heat exchanger 518.
  • Refrigeration in first heat exchanger 518 is preferably provided by expanding high pressure nitrogen (N 2 ) from an elevated pressure air separation unit (not shown) along line 514, expanding the high pressure
  • the intervening process unit is a heat exchanger intended to pre-cool the fuel gas before it is introduced into the expander
  • the present invention advantageously reduces the gasifier pressure for a given acid gas removal refrigeration duty requirement and a given expanded fuel gas pressure requirement set by the gas turbine model.
  • This fiiel gas pre-cooling feature is expected to become especially useful as the gas turbine technology advances with a resultant increase in the gas turbine pressure ratio.
  • This pre-cooled expansion configuration is also expected to broaden the lower operating range ofthe gasifier pressure and thus, increase the number of gasification technologies or gasifier heat recovery options that may take advantage ofthe cold expander invention.
  • the minimum gasifier pressure required without cooling the syn gas prior to expansion is 1080 psia, whereas by cooling it to 45° F, the gasifier pressure is reduced to about 890 psia.
  • the mmimum gasifier pressure required without cooling the syn gas prior to expansion is approximately 1390 psia, whereas by cooling it to 45° F, the gasifier pressure is reduced to about 1140 psia
  • Texaco recommends 1215 psia as the maximum gasifier pressure

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Power Engineering (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

Le groupe de gazéification d'une centrale intégrée gazéification/cycle mixte comporte un groupe de désulfuration (30) qui produit un gaz propre (42) que l'on détend pour assurer la réfrigération (60) du groupe de désulfuration (30). Des réalisations préférées incluent une unité intermédiaire de traitement qui comporte séparateur à membrane (390), un groupe de synthèse (391, 495) ou un échangeur thermique (260) à détente d'azote froid (250) en aval du groupe de séparation d'air (211).
PCT/US1997/005715 1996-04-18 1997-04-08 Integration a synergie d'une unite d'elimination par procede physique des gaz acides de solvants dans des centrales ayant recours a la gazeification WO1997039235A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU24440/97A AU2444097A (en) 1996-04-18 1997-04-08 Synergistic integration of physical solvent agr with plants using gasification

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US63462796A 1996-04-18 1996-04-18
US08/634,627 1996-04-18
US71063196A 1996-09-18 1996-09-18
US08/710,631 1996-09-18

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WO1997039235A1 true WO1997039235A1 (fr) 1997-10-23

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Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1043557A2 (fr) * 1999-04-09 2000-10-11 L'air Liquide Société Anonyme pour l'étude et l'exploitation des procédés Georges Claude Unité intégrée de séparation des gaz de l'air et de production d'énergie
WO2000075499A1 (fr) * 1999-06-03 2000-12-14 General Electric Company Turbodetendeur modifie de gaz combustible, destine a des gazogenes a oxygene pulse, et procede associe
US8141356B2 (en) * 2008-01-16 2012-03-27 Ford Global Technologies, Llc Ethanol separation using air from turbo compressor
US8235024B2 (en) 2007-10-12 2012-08-07 Ford Global Technologies, Llc Directly injected internal combustion engine system
US8245690B2 (en) 2006-08-11 2012-08-21 Ford Global Technologies, Llc Direct injection alcohol engine with boost and spark control
KR20120104106A (ko) * 2011-03-11 2012-09-20 제너럴 일렉트릭 캄파니 기체 처리용 용매를 냉각시키는 시스템 및 방법
US8312867B2 (en) 2007-12-12 2012-11-20 Ford Global Technologies, Llc On-board fuel vapor separation for multi-fuel vehicle
US8375899B2 (en) 2008-05-08 2013-02-19 Ford Global Technologies, Llc On-board water addition for fuel separation system
US8393312B2 (en) 2005-11-30 2013-03-12 Ford Global Technologies, Llc Event based engine control system and method
US8434431B2 (en) 2005-11-30 2013-05-07 Ford Global Technologies, Llc Control for alcohol/water/gasoline injection
US8529679B2 (en) 2009-11-05 2013-09-10 General Electric Company System and method for improving performance of an IGCC power plant
US8550058B2 (en) 2007-12-21 2013-10-08 Ford Global Technologies, Llc Fuel rail assembly including fuel separation membrane

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Cited By (20)

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Publication number Priority date Publication date Assignee Title
EP1043557A3 (fr) * 1999-04-09 2001-04-25 L'air Liquide Société Anonyme pour l'étude et l'exploitation des procédés Georges Claude Unité intégrée de séparation des gaz de l'air et de production d'énergie
EP1043557A2 (fr) * 1999-04-09 2000-10-11 L'air Liquide Société Anonyme pour l'étude et l'exploitation des procédés Georges Claude Unité intégrée de séparation des gaz de l'air et de production d'énergie
WO2000075499A1 (fr) * 1999-06-03 2000-12-14 General Electric Company Turbodetendeur modifie de gaz combustible, destine a des gazogenes a oxygene pulse, et procede associe
US6314715B1 (en) 1999-06-03 2001-11-13 General Electric Co. Modified fuel gas turbo-expander for oxygen blown gasifiers and related method
US8393312B2 (en) 2005-11-30 2013-03-12 Ford Global Technologies, Llc Event based engine control system and method
US8434431B2 (en) 2005-11-30 2013-05-07 Ford Global Technologies, Llc Control for alcohol/water/gasoline injection
US8245690B2 (en) 2006-08-11 2012-08-21 Ford Global Technologies, Llc Direct injection alcohol engine with boost and spark control
US8235024B2 (en) 2007-10-12 2012-08-07 Ford Global Technologies, Llc Directly injected internal combustion engine system
US8495983B2 (en) 2007-10-12 2013-07-30 Ford Global Technologies, Llc Directly injected internal combustion engine system
US8312867B2 (en) 2007-12-12 2012-11-20 Ford Global Technologies, Llc On-board fuel vapor separation for multi-fuel vehicle
US8459238B2 (en) 2007-12-12 2013-06-11 Ford Global Technologies, Llc On-board fuel vapor separation for multi-fuel vehicle
US8550058B2 (en) 2007-12-21 2013-10-08 Ford Global Technologies, Llc Fuel rail assembly including fuel separation membrane
US9038613B2 (en) 2007-12-21 2015-05-26 Ford Global Technologies, Llc Fuel rail assembly including fuel separation membrane
US8141356B2 (en) * 2008-01-16 2012-03-27 Ford Global Technologies, Llc Ethanol separation using air from turbo compressor
US8375899B2 (en) 2008-05-08 2013-02-19 Ford Global Technologies, Llc On-board water addition for fuel separation system
US8656869B2 (en) 2008-05-08 2014-02-25 Ford Global Technologies, Llc On-board water addition for fuel separation system
US8529679B2 (en) 2009-11-05 2013-09-10 General Electric Company System and method for improving performance of an IGCC power plant
KR20120104106A (ko) * 2011-03-11 2012-09-20 제너럴 일렉트릭 캄파니 기체 처리용 용매를 냉각시키는 시스템 및 방법
EP2498033A3 (fr) * 2011-03-11 2018-02-28 General Electric Company Système et procédé de refroidissement d'un solvant pour le traitement de gaz
KR102027584B1 (ko) * 2011-03-11 2019-10-01 제너럴 일렉트릭 캄파니 기체 처리용 용매를 냉각시키는 시스템 및 방법

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