GB2296255A - Production of electricity and hydrogen - Google Patents
Production of electricity and hydrogen Download PDFInfo
- Publication number
- GB2296255A GB2296255A GB9425868A GB9425868A GB2296255A GB 2296255 A GB2296255 A GB 2296255A GB 9425868 A GB9425868 A GB 9425868A GB 9425868 A GB9425868 A GB 9425868A GB 2296255 A GB2296255 A GB 2296255A
- Authority
- GB
- United Kingdom
- Prior art keywords
- stream
- carbon dioxide
- hydrogen
- gas
- pressure
- Prior art date
- Legal status (The legal status 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 status listed.)
- Withdrawn
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
- F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
- F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
- F01K23/067—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle the combustion heat coming from a gasification or pyrolysis process, e.g. coal gasification
-
- 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
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/005—Carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
- C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
- F02C3/20—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
- F02C3/26—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension
- F02C3/28—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension using a separate gas producer for gasifying the fuel before combustion
-
- 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
- C10J2300/1665—Conversion of synthesis gas to chemicals to alcohols, e.g. methanol or ethanol
-
- 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
- C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
-
- 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
- C10J2300/1687—Integration of gasification processes with another plant or parts within the plant with steam generation
-
- 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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
-
- 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
- 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]
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Industrial Gases (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
A process for the production of electricity and hydrogen wherein a carbonaceous fuel is partially oxidised at elevated pressure with oxygen or an oxygen containing gas, the gasification product gas is quenched in water or cooled and mixed with steam, passed through a carbon monoxide shift reactor, passed through a carbon dioxide removal device, and at least a part of this stream then has its pressure reduced and at least a part of the part of the stream which has had its pressure reduced is used first to recover at least some of the carbon dioxide removed and then at least some of the stream containing recovered carbon dioxide is used as a fuel for a gas turbine, and at least a part of the part of the stream not used for carbon dioxide recovery is used as a source of hydrogen with or without further purification.
Description
IGCC/REFINERY UTILITIES UNIT
This invention relates to the production of utilities such as electric power, hydrogen, steam, oxygen, nitrogen, and methanol for a refinery utilising heavy ends (eg refinery residue) as the feedstock.
This invention is a process for the production of electricity and hydrogen wherein a carbonaceous fuel is partially oxidised at elevated pressure with oxygen or an oxygen containing gas, the gasification product gas is quenched in water or cooled and mixed with steam, passed through a carbon monoxide shift reactor, passed through a carbon dioxide removal device, and at least a part of this stream then has its pressure reduced and at least a part of the part of the stream which has had its pressure reduced is used first to recover at least some of the carbon dioxide removed and then at least some of the stream containing recovered carbon dioxide is used as a fuel for a gas turbine, wherein at least a part of the part of the stream not used for carbon dioxide recovery is used as a source of hydrogen with or without further purification.
There are a number of benefits from adding carbon dioxide to the stream which is to be used for fuel gas in the gas turbine: the amount of water needed to be added to effect any given level of NOX control is much reduced: also the temperature of the water needed to add any given amount of water to the stream is lower than would otherwise be the case because the carbon dioxide itself picks up water. This increases the overall thermodynamic efficiency of power production in the plant because heat that otherwise would be used to gain the required level of 'saturation' can then be used to raise higher pressure steam or used to heat the fuel gas fed to the combined cycles gas turbine to an even higher temperature.
Other advantages of this invention are that in addition to the retention of the partial pressure of the carbon monoxide - and the addition that this makes to the mass flow through the combined cycle gas turbine and its flue gas heat recovery section - the removal of some or substantially all of the carbon dioxide from a stream from which a purer hydrogen stream is prepared greatly eases such preparation by means such as molecular sieve pressure swing adsorption (PSA) or membrane purification.
Refineries produce high sulphur residues the disposal of which is becoming more difficult because of environmental legislation. As similar legislation also restricts the sulphur content of refinery products, refineries are needing more and more hydrogen for desulphurisation. Gasoline reformulation is also causing changes to refinery operations.
Refineries require several other utility services for refining crude oil.
Naturally electricity is required, as is oxygen for the Claus unit, nitrogen for tank blanketing, steam for many heating duties, and sulphur free fuel gas.
One means of producing these utilities is through the partial oxidation vgasification) under elevated pressure of low quality waste hydrocarbons which may or may not be produced in the refinery.
The raw gasification product gas consists mainly of equal quantities of carbon monoxide and hydrogen together with about ten percent of carbon dioxide. In order to maximise the production of the more desired product hydrogen, the raw gasification gas, after quenching with water or cooling and the addition of steam, is passed through a bed of catalyst wherein the reaction between carbon monoxide and steam occurs producing more hydrogen and carbon dioxide (the so called water gas 'shift' reaction). This may be effected before or after the removal of sulphur compounds from the stream.
The hydrogen required for eg hydrotreating and the fuel needed for electricity generation and other uses can then be prepared from this stream.
The electricity alternator can be driven by a gas turbine fuelled by the fuel stream. Such a turbine may form a part of a combined cycle system to enhance the efficiency of power generation, and steam production.
The is a problem in extracting the hydrogen from the gas stream without significant loss of useful energy. There are a number commercial processes such as membrane technology and pressure swing adsorption using molecular sieves which will separate the hydrogen from the gas, or liquid wash systems which will preferentially remove the carbon dioxide leaving a high hydrogen concentration in the washed gas. However it is desirable to keep both the hydrogen and the fuel gas at pressure, and if some of the fuel gas is to be used as a gas turbine fuel it is also desirable for the carbon dioxide to be part of that fuel in order to have a lower flame temperature which has the effect of lowering the NOX formation, and, because it is a high molecular weight gas, to be expanded to atmospheric pressure to produce useful shaft energy.
The available commercial processes referred to significantly reduce the pressure of a substantial part of either the hydrogen or carbon dioxide often making energy-consuming gas compression necessary if the low pressure gas is to be used as a fuel or processing material. This invention enables a substantial part of the carbon dioxide in the shifted gasification gas to be placed selectively in a fuel gas stream with minimum loss of its partial pressure for use as a gas turbine fuel whilst leaving the remaining hydrogen rich gas at substantially its original pressure. Typically the carbon dioxide may be recovered at more than 35% of its original partial pressure, often at more than 50%, sometime more than 60% and even more than 70%, or 75%.
Preferably the carbon dioxide is removed from the source stream by use of a physical or physical/chemical system or a molecular sieve system operated with a back-pressured ventilated system on the recovery side. The ventilating stream being the stream that is to become the fuel gas stream.
Preferable the carbon dioxide is removed from the source stream by means of a physical solvent, the carbon dioxide-rich solution being then passed down a column maintained at a pressure with degassing aided by the use of a stripping gas - the stream into which the carbon dioxide is to be added.
The amount of carbon dioxide removed depends on a number of factors the main one being the hydrogen purity required, and whether or not additional hydrogen purification is to be effected. If no further hydrogen purification steps are to be used then, within the technology of known means, particularly known physical solvent means, substantially all of the carbon dioxide can be removed.
If a partial pressure swing (ventilated) molecular sieve adsorber is used then the amount of carbon dioxide removed will be calculated according the economics of such systems.
The source stream is a stream from or derived from partial oxidation of a carbonaceous material such as refinery residue, coal, Orimulsion (TM) and other carbonaceous wastes such as sewage sludge.
Preferably the stream from the partial oxidation reactor is quenched in the well known manner originally patented and licensed by Texaco
Development Corporation. The quenched stream is, maybe after some temperature adjustment, passed through a carbon monoxide and steam (water gas shift) catalyst bed wherein some of the carbon monoxide contained in the stream is reacted with the steam to form carbon dioxide and (additional) hydrogen. By means of the shift reaction the amount of carbon dioxide in the source stream is increased thereby making it easier to remove in that for a given pressure of the source stream, the partial pressure of the carbon dioxide in that stream is increased - thus increasing the equilibrium or load carrying capacity of the physical solvent.Likewise the increase in partial pressure would increase the loading attainable on any molecular sieve used for the purpose of removing the carbon dioxide. Naturally an increase in the partial pressure in the source stream increases the pressure at which the carbon dioxide can be recovered into the stream into which it is destined to be added/mixed.
The pressure at which the partial oxidation takes place is above 30, bara, preferably above 40 bara, more preferably above 45 bara, more preferably above 50 bara, more preferably above 55 bara, and most preferably above 60 bara.
The pressure drop through which the carbon dioxide-depleted stream passes is preferably effected in a turbine for the recovery of shaft power.
It would be possible to expand the stream (preferably after drying it) from a comparatively cold temperature such that the stream falls below say 10 degrees celsius. The resulting cold stream could then be used as a source of
olth - particularly in the carbon dioxide removal unit. Alternatively it would De possible to heat the stream to be expanded such that in an expander it gives out more power.
The pressure drop through which the carbon dioxide depleted stream passes is more than 5 bar, preferably above 10 bar, more preferably above 15 bar, more preferably above 20 bar, and most preferably above 25 bar.
Regarding the pressure drop which could be effected on the hydrogen stream just after it is split from the fuel gas stream: it should be noted that it notwithstanding the fact that the hydrogen may be wanted at a high pressure, because of the efficiency and cost of further hydrogen stream processing, notably any PSA unit, it may be desirably to reduce the pressure of any feed to a PSA stream to the economic level inclusive of the cost of any recompression of the hydrogen further purified hydrogen stream. PSA units are often most economic at about 30 bar.
A plant incorporating the process of the invention might comprise (see
Fig 1): a partial oxidation reactor (1) to which is fed a carbonaceous fuel and oxygen. A quench (2) into which the very hot gases are fed causing a substantial amount but not all of the water to evaporate. A trim boiler (3) (not to be confused with a very hot gas boiler that would be located directly on the outlet of the partial oxidation reactor). A shift - reactor preheater (4) followed by the shift reactor (5). Next would follow a number of gas coolers (items 6 to 9) to further cool the raw gas and heat streams and raise steam and through a final cooling water cooler(10).The gas would then flow through a sulphur compounds removal unit (11) wherein sulphur compounds would be removed from the stream and concentrated into a stream that would be fed to a Claus unit (not shown) for the conversion of the sulphur compounds into elemental sulphur. The substantially sulphur free stream could then have a side stream taken from it for eg the production of methanol. Next the stream would flow though a carbon dioxide removal column (12) wherein at least some of the carbon dioxide would be removed into a physical solvent. The carbon dioxide depleted stream is split into two streams the one destined to be the fuel gas stream is next passed through an expander (13) to produce shaft power. The other stream is passed to a pressure swing adsorption unit (14) to further purify the hydrogen, the off gases being used as a clean fuel gas stream.The stream from the expander is then used as a stripping gas in stripping a column (15) to recover the carbon dioxide from the physical solvent. The combined recovered carbon dioxide/ fuel gas stream is then passed up a saturator column (16) to add the amount of steam required to keep the burning characteristics of the fuel gas such that the NOX produced when this gas is burnt is below that allowed by local regulations. The 'saturated' gas is then used a fuel for the gas turbine in the combined cycle unit (17).
In another embodiment it would be desirable to raise high pressure steam from the stream from the shift reactor, and also to raise lower pressure steam just after - preferably at the same pressure as the steam raised in the trim boiler located downstream of the whole gasification unit (following quench as cleanup.
Preferably having shifted the gas from the partial oxidation reactor, the stream may be passed through a sulphur removal unit. Such unit may employ either hot or cold known means of removal such as the use of methanol as a solvent.
Following the removal of sulphur and at least some of the carbon dioxide, the stream may undergo a second stage of carbon monoxide water gas shift reaction - preferably employing a low temperature shift catalyst such as that supplied by ICI. If a second carbon monoxide shift stage is employed, the residual sulphur compounds may be removed from its feed by the use of a bed of zinc oxide or any other known means. The carbon dioxide thereby produced may similarly be removed giving a substantially pure stream of hydrogen whose main impurities are methane and residual carbon monoxide.
If necessary these may be removed by the use of a bed of molecular sieves to give a highly pure stream of hydrogen.
After the sulphur removal section, a side stream may be taken for the production of chemicals requiring 'synthesis gas as a feedstock - especially for methanol production.
Claims (4)
1) A process for the production of electricity and hydrogen wherein a
carbonaceous fuel is partially oxidised at elevated pressure with oxygen
or an oxygen containing gas, the gasification product gas is quenched
in water or cooled and mixed with steam, passed through a carbon
monoxide shift reactor, passed through a carbon dioxide removal
device, and at least a part of this stream then has its pressure reduced
and at least a part of the part of the stream which has had its pressure
reduced is used first to recover at least some of the carbon dioxide
removed and then at least some of the stream containing recovered
carbon dioxide is used as a fuel for a gas turbine, and at least a part
of the part of the stream not used for carbon dioxide recovery is used
as a source of hydrogen with or without further purification.
2) A process as claimed in claim 1 in which the stream containing the
recovered carbon dioxide is contacted with liquid water so as to add
steam to the gaseous stream.
3) A process as claimed in Claim 1 wherein the partial oxidation is carried
out above 30 bara.
4) A process as claimed in Claim 1 wherein the pressure reduction is
greater than 5 bar 5) A process as claimed in Claim 1 wherein the pressure reduction is
carried out through a expansion turbine to recover useful power.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB9425868A GB2296255A (en) | 1994-12-21 | 1994-12-21 | Production of electricity and hydrogen |
| PCT/GB1995/002993 WO1996019642A1 (en) | 1994-12-21 | 1995-12-21 | Igcc/refinery utilities unit |
| AU42699/96A AU4269996A (en) | 1994-12-21 | 1995-12-21 | Igcc/refinery utilities unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB9425868A GB2296255A (en) | 1994-12-21 | 1994-12-21 | Production of electricity and hydrogen |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| GB9425868D0 GB9425868D0 (en) | 1995-02-22 |
| GB2296255A true GB2296255A (en) | 1996-06-26 |
Family
ID=10766333
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB9425868A Withdrawn GB2296255A (en) | 1994-12-21 | 1994-12-21 | Production of electricity and hydrogen |
Country Status (3)
| Country | Link |
|---|---|
| AU (1) | AU4269996A (en) |
| GB (1) | GB2296255A (en) |
| WO (1) | WO1996019642A1 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1998027004A1 (en) * | 1996-12-19 | 1998-06-25 | Siemens Westinghouse Power Corporation | Goal gasification and hydrogen production system and method |
| EP0964829A1 (en) * | 1997-09-12 | 1999-12-22 | Texaco Development Corporation | Removal of acidic gases in a gasification power system with production of hydrogen |
| US6421721B1 (en) | 1999-01-05 | 2002-07-16 | International Business Machines Corporation, | Controlling device access in a network |
| WO2004042200A1 (en) * | 2002-11-08 | 2004-05-21 | Alstom Technology Ltd | Gas turbine power plant and method of operating the same |
| US7503947B2 (en) | 2005-12-19 | 2009-03-17 | Eastman Chemical Company | Process for humidifying synthesis gas |
| WO2009105305A2 (en) * | 2008-02-21 | 2009-08-27 | General Electric Company | Methods and systems for integrated boiler feed water heating |
| EP2320049A3 (en) * | 2009-11-10 | 2017-06-21 | Mitsubishi Hitachi Power Systems, Ltd. | Gasification power generation system provided with carbon dioxide separation and recovery device |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10053778A1 (en) * | 2000-10-30 | 2002-05-08 | Alstom Switzerland Ltd | Production of synthesis gas containing hydrogen and carbon monoxide, especially for methanol production, uses thermodynamic cycle to recover much of enthalpy of gas leaving reformer at high temperature and pressure |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2196016A (en) * | 1986-08-29 | 1988-04-20 | Humphreys & Glasgow Ltd | Clean electric power generation process |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3414140A1 (en) * | 1984-04-14 | 1985-10-24 | M.A.N. Maschinenfabrik Augsburg-Nürnberg AG, 8000 München | Method and device for operating a gasification reactor |
| US4936869A (en) * | 1984-04-24 | 1990-06-26 | Minderman Peter A | Liquid hydrogen polygeneration system and process |
-
1994
- 1994-12-21 GB GB9425868A patent/GB2296255A/en not_active Withdrawn
-
1995
- 1995-12-21 WO PCT/GB1995/002993 patent/WO1996019642A1/en active Application Filing
- 1995-12-21 AU AU42699/96A patent/AU4269996A/en not_active Abandoned
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2196016A (en) * | 1986-08-29 | 1988-04-20 | Humphreys & Glasgow Ltd | Clean electric power generation process |
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5955039A (en) * | 1996-12-19 | 1999-09-21 | Siemens Westinghouse Power Corporation | Coal gasification and hydrogen production system and method |
| WO1998027004A1 (en) * | 1996-12-19 | 1998-06-25 | Siemens Westinghouse Power Corporation | Goal gasification and hydrogen production system and method |
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Also Published As
| Publication number | Publication date |
|---|---|
| AU4269996A (en) | 1996-07-10 |
| WO1996019642A1 (en) | 1996-06-27 |
| GB9425868D0 (en) | 1995-02-22 |
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