CN103380198A - Method for utilizing thermal energy of product gases in a BtL plant - Google Patents

Method for utilizing thermal energy of product gases in a BtL plant Download PDF

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CN103380198A
CN103380198A CN2011800648305A CN201180064830A CN103380198A CN 103380198 A CN103380198 A CN 103380198A CN 2011800648305 A CN2011800648305 A CN 2011800648305A CN 201180064830 A CN201180064830 A CN 201180064830A CN 103380198 A CN103380198 A CN 103380198A
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making
biomass
steam
gas
oilmill
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J·考托
O-P·维尔亚凯宁
M·蒂莫宁
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Vapo Oy
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Vapo Oy
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    • 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
    • C10J3/72—Other features
    • C10J3/86—Other features combined with waste-heat boilers
    • 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
    • C10J3/72—Other features
    • C10J3/726—Start-up
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00—Methods of steam generation characterised by form of heating method
    • F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
    • F22B1/1838—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines the hot gas being under a high pressure, e.g. in chemical installations
    • F22B1/1846—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines the hot gas being under a high pressure, e.g. in chemical installations the hot gas being loaded with particles, e.g. waste heat boilers after a coal gasification plant
    • 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
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • 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
    • C10K1/02—Dust removal
    • C10K1/024—Dust removal by filtration
    • 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
    • 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]
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/40—Solid fuels essentially based on materials of non-mineral origin
    • 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
    • F01K13/00—General layout or general methods of operation of complete plants
    • 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
    • F01K17/00—Using steam or condensate extracted or exhausted from steam engine plant
    • F01K17/06—Returning energy of steam, in exchanged form, to process, e.g. use of exhaust steam for drying solid fuel or plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
    • F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
    • F22D1/32—Feed-water heaters, i.e. economisers or like preheaters arranged to be heated by steam, e.g. bled from turbines
    • 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
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming 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
    • C01B2203/02—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
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • 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
    • 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
    • C01B2203/06—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
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • 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
    • C10J2300/0903—Feed preparation
    • C10J2300/0909—Drying
    • 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
    • C10J2300/0916—Biomass
    • 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
    • C10J2300/0959—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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1621—Compression of synthesis gas
    • 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
    • C10J2300/1687—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
    • Y02E20/14—Combined heat and power generation [CHP]
    • 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
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • 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
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • 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
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    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

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Abstract

The invention for utilizing thermal energy of gases generated in a BtL plant. The characterizing feature of the invention is that the thermal energy of discharge gas streams generated in the BtL plant is used for driving various compressor machineries and/or electricity generation, whereby the plant can operate as a stand-alone facility.

Description

Be used for utilizing the method for the heat energy of the gas that the biomass-making oilmill produces
Technical field
The present invention relates to a kind of method of the heat energy for utilizing the gas that produces at the biomass-making oilmill as described in the preamble according to claim 1.The invention still further relates to application according to claim 9.
Background technology
In the biomass-making oilmill that uses prior art, gasifying solid biomass in high temperature or low temperature gasification device.The function of biomass-making oilmill is usually synthetic by Fischer-Tropsch and biomass are changed into liquid fuel (biomass are to liquid) by synthetic gas.In high-temperature gasification, gasifier is being higher than the lower running of grey melt temperature (more specifically being at approximately 1200-1400 ℃).According to employed technology, generating gasification under the pressure of 1-40bar.At present, technology is developed, to be particularly suited under the gasifier pressure of about 5bar biomass being carried out high-temperature gasification.
Purified gas that produce in gasification and further is commonly referred to as synthetic gas, and this is subsequently for the preparation of other product such as ammonia or long-chain aromatic hydrocarbon because of synthetic gas.
In making synthesising biological fuel, the material synthesis gas that in gasification, produces must be cooled and purifying to remove dust, thus, other component except hydrogen and carbon monoxide need to be isolated from gas stream.The pure synthetic gas that produces, (that is, hydrogen and carbon monoxide) is sent to fischer-tropsch reactor (FT reactor), wherein, produces paraffinic hydrocarbon existing in the situation of catalyzer.Usually at the pressure of 20-40bar and under about 200 ℃ temperature, carry out Fischer-Tropsch FT and process.The wax-like product that obtains thus is called as biological wax.
Processing the biological wax that obtains from FT need to further refine by for example hydrogenization, cracking and distillation, is suitable for the fuel that engine uses to be produced by biological wax.And, under the pressure (30-80bar) that raises, carry out these processing.Hydrogenization refers in the hydrogen environment and processes, and wherein, the two keys between the carbon are saturated.Correspondingly, cracking refers at the long hydrocarbon chain of reactor Fracture.Distillation is last so that fuel fraction is separated from one another, thereby produces diesel oil fuel, petroleum naphtha, kerosene, liquefied petroleum gas (LPG) etc.
If under the pressure of the pressure that is lower than FT processing and refinement processing, gasify, then the pressure of necessary rising synthetic gas.Traditionally, implement described step at cooling syngas and after filtering with the removal solid impurity.Realize that by the gas compressor of obtainable number of different types pressure raises.Typically, described gas compressor can be classified as axial compressor, radial compressor, reciprocating compressor and screw-type compressor.More usually, implement the synthetic gas compression with axial compressor and radial compressor.Select suitable type of compressor based on required pressure rising, gaseous fraction and volume.
The common trait of compressor is that they are rotating equipments.Compress required mechanical energy and typically derive from electric motor, perhaps alternately, from steam turbine or gas turbine.For example, under about 5bar to 35bar pressure, has the power input that synthetic gas compression in the biomass-making oilmill of vaporising fuel power of 300-500MW needs about 10-17MW.
What replace air is, gasifies with oxygen, and described oxygen must be pressurized to be used for gasification process.By at first air cooling is become liquid form and then air distillation gas is separated from each other and prepares oxygen by air.For the synthesis gas equipment of 300-500MW vaporising fuel power, the compressor power of air gas equipment is 10-15MW.In breathing equipment, in cooling process and oxygen pressure be increased in the gasification process pressure and need compressor.
In the biomass-making oil treatment, pressure reduces towards the downstream of processing exit end after pressurization steps.This is owing in the stage pressure-losses occurs in different treatment in the mode of accumulating.If be desirably in reverse supply gas stream in the processing, then must be by compressing the stress level of this gas stream that raises.Yet these compressors power for making the required compression horsepower of main gas stream motion is lower, and typically each compressor is about 200-700kW.
And, if processing comprises in order to catch carbon monoxide carbon monoxide is liquefied, then before being cooled to-50 ℃, the gaseous state carbon monoxide its pressure must be increased to about 20bar by means of heat exchanger and expansion valve.Be that carbon monoxide compression in the biomass-making oilmill of 300-500MW and the power input demand of cooling apparatus compressor are about 10-15MW at gasified fuel power, the liquefaction amount of carbon monoxide is about 50-75t/h thus.
As it is evident that from above discussion, a lot of different compressors consume the major part in the required electric energy of biomass-making oilmill.Therefore, although the biomass-making oilmill has the possibility of generating electricity according to its processing with the steam resource in factory, factory still depends on external power.
Summary of the invention
The present invention compresses mainly for synthetic gas, but more generally, the present invention can be applied to other purposes, for example, is applied to the treatment step that needs compression mentioned above.
Must be noted that at this biomass-making oil treatment produces saturation steam at different stress level (especially under high pressure) by the cooling material synthesis gas and to himself purifying.More specifically, the synthetic controlled cooling of Fischer-Tropsch (FT) in-discharge a large amount of saturation steams under the high pressure.Except the personal demand of the relatively small amount of biomass-making oil treatment self, in factory, the main maximum consumption person of back pressure steam is that biomass are dry.But, the biomass-making oilmill has the abundant intrinsic supply of low-pressure steam.
Typically, for above-mentioned reasons, purpose be so that the biomass-making oilmill with can use it to cross fumy industrial equipments to combine.Advantageously, for example make paper, paper pulp and fiber board dry and in the heat supply in area and generating, use steam.Reduced fuel consumption with the combined factory of described biomass-making oilmill from the obtainable steam of biomass-making oilmill.
Yet consequent problem is: find that combined suitable factory is to the formation major limitation for practicable a plurality of possible positions of building the biomass-making oilmill.Because the biomass-making oilmill must be arranged in plant location before do not have the remaining area of intended purpose, so that the layout of biomass-making oilmill becomes usually is not good enough.It is the favourable places of biomass-making oilmill that the better combined factory location of logistics support there is no need.
And, it should be noted that, biomass-making oilmill and the factory combined with it must be constructed to be permeable to tackle these constraint condition, and described constraint condition is that in equipment/factory any one do not have continued running, this means that they all need to be equipped with independent facility.Therefore, the combined overall cost of ownership that must not cause is cut down, but on the contrary, combined facility and the processing of independent operation need to be set.
Should utilize most effectively the steaminess of crossing that in independent situation, produces---described situation need to be generated electricity by means of steam turbine when shortage steam consumption person.Yet it is impossible using saturation steam in turbine, unless by for example in independent overheated boiler combustion of gaseous fuel make saturation steam overheated, and the unit that described independent overheated boiler is redundancy in this processings.
The invention provides now a kind of layout that can overcome the problems referred to above.Purpose of the present invention relates to a kind of situation, wherein, exists simultaneously electricity shortage and saturation steam too much in the biomass-making oil treatment.Need electric power to being powered by electric motor driven various compressors.Simultaneously, steam is sent to processing or the power equipment of combined factory, wherein, and steam driven turbine and generating electricity.The part of this electric power can return to use in the biomass-making oil treatment.
In an embodiment of the present invention, basic goal is the local use excess steam and the electric power amount of buying is reduced.Come the drive compression machine can make these two targets combined by being used in the steam that produces in the processing of biomass-making oilmill.Thereby, make mechanical energy change into electric energy and again change into mechanical transformation of energy loss to minimize.For for using steam in the turbine, at first must make steam superheating.Next will describe a kind of method, wherein, realize making steam superheating by means of the treatment facility that is called as steam reformer.
Steam reformer is a kind of unit, and described unit is applied in the petroleum refining industry to be used for producing hydrogen from methane and heavy hydrocarbon fraction usually, thereby is used in the oil refining.By means of suitable catalyzer and at high temperature by steam supply is realized reforming in the gas of just being reformed.This processing is also referred to as english term Steam Methane Reformer(SMR(steam methane reformer)) or Steam Reformer Unit(SRU(steam reformer unit)).
Next describe a kind of method, wherein, it is overheated to realize with the SMR technology.The material synthesis gas that results from the gasifying stage of biomass-making oil treatment comprises the hydrogen that FT processes that is used for of non-capacity.Therefore, it is essential carrying out the hydrogen interpolation based on the gas shift reaction that is called as water-gas shift technology (WGS=water-gas shift).In this is processed, carbon monoxide (CO) is isolated from the synthetic gas that produces gasification, spray steam in the gas stream, and in ensuing catalyzed reaction, produce as follows hydrogen:
CO+H 2O→CO 2+H 2
The FT of biomass-making oilmill processes and the different steps of oil refining produces various tail gas, use the SMR technology can be from described various tail gas recover hydrogen.Thus, be to compare such as the such situation of the fossil resource of methane with sources of hydrogen, thereby improved the output of biomass-making oil treatment and so that produced hydrogen (that is, deriving from biomass) more economically.
Tail gas comes from the biomass-based raw material of equipment and comprises different types of light hydrocarbon, and described tail gas is freely translated into Finnish and produced for " rear-end gases " and in Fischer-Tropsch processing and post-processing stages subsequently.Traditionally, use the SMR technology to produce hydrogen by the methane of Sweet natural gas:
CH 4+H 2O→CO+3H 2
Now, this technology is applied to the tail gas of generation in FT processes.Therefore, reform as follows such as the gas molecule with long-chain of propane:
C 3H 8+3H 2O→3CO+7H 2
Can in processing, further utilize carbon monoxide via the WGS reaction thus:
CO+H 2O→CO 2+H 2
Therefore, can utilize WGS and/or SMR to process to replenish the biomass-making oil treatment, be used for to improve output and to adjust the ratio of hydrogen and carbon monoxide.With regard to methane, for example, total reaction is:
CH 4+2H 2O→CO 2+4H 2
In order in pressure turbine, to use the high-pressure saturated steam of the material synthesis gas that is derived from gasifier, must make described steam superheating, this is because there is not water of condensation can be sent to turbine during vapor expansion.In independent overheated boiler or can realize overheatedly by the hot fuel gas of steam reformer, the hot fuel gas of described steam reformer more suitably is suitable for the biomass-making oil treatment.Carry out the reformation to the tail gas of FT processing in reformer, described tail gas comprises the mixture of different hydrocarbon.The temperature of the gas of just being reformed is by making a part of gas in the boiler or some other fuel combustion and typically be increased to about 900-1100 ℃.
Treatment temp is so high, so that the flue gas of discharging still can be used for making steam superheating, this means and can realize making steam superheating with the minimum extra investment for the SMR technology need not to install in the situation of boiler.Because flue gas is derived from ashless tail gas (that is, being derived from discharging gas and residual gas), so described flue gas cleans.Significantly, can also use the outside fuel of supplying with (such as other inflammable gas of Sweet natural gas or the processing of biomass-derived liquefaction) to heat the SMR unit.
Excessive back pressure steam can be converted into electric power in the vapor condensation turbine.The condensation turbine can be the equipment of a platform independent or be combined into one with the synthetic gas turbo-driven compressor.Moreover back pressure turbine can be independent of compressor, thereby helps the complete independent operation of compressor and turbine.
Described layout allows more to effectively utilize whole processing chain.Essential characteristic of the present invention is the key factor in method and the application thereof.More specifically, the invention is characterized in the content described in each claim.
Description of drawings
Hereinafter, 1-3 describes the present invention in further detail by means of preferred embodiment by the reference accompanying drawing, in described accompanying drawing:
Fig. 1-3 shows the process flow diagram for the layout of implementing the method according to this invention.
Embodiment
Fig. 1 shows for the schematic flow sheet of being produced biofuel by solid biomass.Supply to that biomass 12 in the processing are dried and its particle size is uniformity in pre-treatment of raw material step 1, to be suitable for supplying to gasifier.It is oxygen gasified 3 to carry out to supply with pretreated biomass, and described oxygen gasified 3 have so that the tar component of gas decomposes such high temperature fully.The decomposition of tar component is for preventing that their condensations in the treatment facility of gasification step downstream part from being necessary.Preparation is processed and is used oxygen in breathing equipment 2.
In step 4, cool off material synthesis gas 28 and in processing 5, filter material synthesis gas to remove dust.Subsequently, can gaseous tension be increased to FT reactor 8 needed levels by compressor 24.Before supplying to the FT reactor, in WGS reactor 6, to adjust carbon monoxide in the gas and the ratio of hydrogen, and other gaseous component and catalyzer poison 7 are isolated from synthetic gas, this other gaseous component and catalyzer poison are split into stream 22.The biological wax that is derived from the FT processing is become to be suitable for the cut 15 of different application by post-processed in refining equipment 9, such as biofuel.
Carry out the cooling of material synthesis gas 28 by means of heat exchanger in processing 4, the water 20 that high pressure is introduced is sent to described heat exchanger.In heat exchanger, water is evaporated to steam and is moved out of with state of saturation.When device start begins, gasification 3 performance functions rather than the downstream stages 6-9 performance function of processing.This means such as the replacement scheme 26a of Fig. 1 shownly, saturation steam must be sent to back pressure net 38 via reducing valve 25.This operational stage must continue a very long time, until receive pure synthetic gas in compressor 24.Hereinafter, can start compressor with the synthetic gas 27 of output squeezing.
If compressor and turbine for good and all are connected to each other by common axis, namely, force described compressor to rotate each other with friction-motion speed with identical speed or via wheel box with turbine, when the motor drive machine, a small amount of cooling steam must be transferred into turbine.
If turbine 23 is designed to be driven by saturation steam, then steam can lead to turbine via the path via line shown in the regional 26b among Fig. 1.Yet because pressure turbine is not designed to receive saturation steam usually, in this case, steam is sent to the back pressure net a very long time via path 26a, until steam reformer 10 becomes to be operable as and ends during by the motor drive compressor.Subsequently, saturated steam flowing is directed to the shown path of regional 26c of Fig. 1.
In Fig. 2, show the layout of the steam flow net of the processing relevant with the present invention.Wherein, the saturated steam flowing 26c of Fig. 1 transmits via superheater 33, thus, produces the flow of superheated steam 39 that is suitable for supplying to turbine 23.
When same axle was connected, it also can be used as independently machine run at saturation steam condensation turbine 24b and pressure turbine 24a and compressor 23.Each machine is operated in the Special Circumstances independently of one another and when starting permission equipment have better behaviour in service.In the processing of time period of runs steadily one elongated segment, usefulness and cost of investment with system of fixture construction will be more favourable.
With regard to back pressure steam 38, the biomass-making oil treatment is basically self-sustaining.Can be for example in the condensed steam generating or in such as those the hot dense process in paper mill or the chemical plant, can use excess steam.When vapor condensation turbine 24b and pressure turbine 24a were installed on the same axle, when the combined power of turbine 24a and 24b surpassed the required power demand of compressor 23, the synchronous motor 34 that is installed on the same axle also can be fulfiled the function of generator.
Since because of winter biomass moisture content higher and make air dried outdoor temperature lower, institute is so that biomass drying 37 consumes steam in the winter time is to consume three times of steam in summer, so excessive back pressure steam 38 changes from winter to summer.With season irrespectively, remain unchanged from the output of the saturated high pressure steam 26 of gasifier and other steam of originating from biomass-making oil treatment 35.In case of necessity, for example, also can be supplied to the back pressure steam net of biomass-making oilmill from other excess steam stream of the back pressure steam net 36 of pulp mill.
In equilibrium state, all obtainable high pressure steam 26 all are sent to back pressure steam net 38 via pressure turbine 24a.Excess steam is transferred into vapor condensation turbine 24b and subsequently condensation in condenser 30.If inadequate by the cooling power that the vapor condensation turbine provides, then can in the auxiliary cooler 31 that is connected with the water route, cool off excess steam.Condensation product 29 turns back in the processing as introducing water 20.
In Fig. 2, also show the intercooler unit 32 for the just compressed synthetic gas 28 of cooling.According to employed technology, the quantity in intercooling stage can be a plurality of, for example, and 4-6.If water temperature is enough high, advantageously be approximately+50 ℃ or higher, then can utilize the warm current water outlet of side cooler, for example be used for the biomass material of dried biomass liquefaction factory.
In Fig. 3, show the schema of processing according to SMR of the present invention.With steam 40b, the inflammable gas 16a that does not utilize in processing is supplied to SMR reactor 10, and this SMR reactor is heated by the waste gas 16b of burning PSA unit and the part of Purge gas 44b by means of combustion air 13.This is processed and produces reformed gas 17, and hydrogen is isolated from described reformed gas after cooling in PSA unit 42.
PSA exit gas or Purge gas 44 also comprise via line and lead to the SMR unit as the inflammable gas of fuel.PSA(namely, the pressure-variable adsorption reactor) be a kind of unit that can the gas of different molecular weight is separated from each other, for example usually hydrogen 43 is separated from the gas mixture that is made of carbonic acid gas and hydrogen.
Can also be by by means of recycle compressor 11 synthesis gas that has the compressed stream 27 that reformate stream is supplied to as shown in Figure 1 being processed in the situation that does not have the PSA unit.
The outlet flue gas 18 that leaves from SMR10 and reformed gas 17 be heat and comprising enough energy under the hot conditions to be enough among superheater 33a and 33b, the making saturation steam 26c that leaves gasifier overheated thus.For example, the saturation steam under 90bar pressure has about 305 ℃ temperature.In order to supply to turbine, temperature also must be increased to about 500 ℃.When in case of necessity, can 20 spray 41 temperature of regulating superheated vapour in the vapour stream by supplying water.
After leaving high-pressure superheater 33a and 33b, the temperature of flue gas 18 is still quite high, thereby allow to utilize flue gas on boiler 46a and superheater 46b, under low pressure to produce steam 40, with the water of heating for dried biomass, the perhaps combustion air in the SMR unit in alternately preheating 47 heat exchangers 45.The flue gas that has cooled off can be disposed to chimney 19.
In aforesaid way, the present invention is directed to a kind of methods and applications of novelty, described methods and applications can utilize the heat energy of the gas that forms in the biomass-making oilmill, be used for using in factory.Described method provides significant benefit, more particularly make steam superheating by the heat energy that utilizes the gas stream in the biomass-making oilmill, produce, drive the turbine of biomass-making oilmill and be used for aftertreatment tail gas so that the maximum production of equipment the finished product being used for.
Compressor and/or generator treatment stage of driving the biomass-making oilmill by the vapour stream of using generation in the biomass-making oilmill is processed by steam turbine are realized described purpose, it is overheated to be undertaken by the flue gas of steam reformer (that is the SMR reactor 10 that, is combined into one with biomass-making oilmill equipment) on the described biomass-making oilmill treatment principle.In addition, by 42 place's recover hydrogen 43 make the output of a factory maximization in the PSA unit.
By this way, the saturated steam flowing supercharging of leaving the biomass-making oil treatment is improved the self-supporting electrobalance of biomass liquefactions significantly and helped the biomass-making oilmill as the self-sufficient running that is independent of the independent facility of another industrial equipments or electric power utility.
According to the present invention, the method that combines with the biomass-making oilmill is used for utilizing the flue gas 18 of steam reformer 10 and/or the heat energy of reformed gas 17, so that the steam superheating 39 of in the biomass-making oilmill, using, to be used for driving synthetic gas turbo-driven compressor 23,24 and/or generating and raising hydrogen output 43, thus, comprise that WGS processes, and makes steam reformer 10 be connected to PSA unit 42.
The biomass-making oilmill is processed at its FT and is produced different FT tail gas in 8, namely, be transferred into the processing waste gas 16 of steam reformer 10, wherein FT tail gas is reformed 17, so that the hydrocarbon polymer of gas 17 is reformed into hydrogen 43 and basically is reformatted into carbon monoxide and further is reformatted into thus carbonic acid gas 44, gas stream cools off after 33,46 in PSA unit 42, from recover hydrogen 43 wherein, so, entrap bubble 44 is recirculated to steam reformer 10, to be used for that steam reformer 10 is heated to about 800-1100 ℃ suitable temp.In order to cool off, the reformed gas 17 in the steam reformer 10 and the flue gas 18 that leaves steam reformer 10 are sent to heat exchanger 33, thus, the heat energy of gas stream is used for making the saturated high pressure steam 26c that leaves gasifier overheated.By this way, utilize the heat energy of the gas that in the biomass-making oilmill, produces to come so that be used for driving the gas superheat of the turbine of biomass-making oilmill.
As mentioned above, this processing has produced a large amount of saturated steam flowings, and for example, those are derived from the saturated steam flowing of gasifier shell of tank or synthesis gas stream.According to the present invention, can realize making these gas superheat by means of the hot gas that in processing, produces (such as, the flue gas of steam reformer).Overheated is fully necessary for making steam can use and be further used for the drive compression machine in turbine.Therefore, the present invention may avoid buying the independently demand of overheated boiler.
Another significant benefit is can build factory and needn't make near another factory (such as, the paper mill that for example can use saturation steam) is positioned at.Now, the method according to this invention allows the power station to combine with this processing.And, saturation steam can be applicable to other processing (such as, make paper and pulp dryer) in, perhaps be applied to produce the heat energy of district heating.
It will be apparent to one skilled in the art that the present invention is not limited to above-mentioned exemplary embodiment, but can in the invention spirit and scope of appended claim, change.

Claims (13)

1. for the method for the heat energy that utilizes the gas that produces at the biomass-making oilmill, it is characterized in that the heat energy of the gas that produces is used for making steam superheating, to drive the turbine of described biomass-making oilmill in the production of described biomass-making oilmill is processed.
2. method according to claim 1, it is characterized in that, in described method, driven compressor and/or the generator in factory processes stage by steam turbine with vapour stream, described vapour stream produces in described biomass-making oilmill is processed and makes described vapour stream overheated by the flue gas of steam reformer, described steam reformer is steam methane reformer reactor (10), the equipment of described steam methane reformer reactor and biomass-making oilmill is combined into one, in addition, for the maximum production of the finished product that make described biomass-making oilmill, by means of pressure-variable adsorption reactor unit (42) recover hydrogen (43).
3. method according to claim 1 and 2, it is characterized in that, in described method, make the overheated self-supporting electrobalance that increases significantly the biomass liquefactions of the saturated steam flowing that in the biomass-making oil treatment, produces, and help the conduct of biomass-making oilmill to be independent of the autonomous running of independent facility of another industrial plant or electric power utility, and make simultaneously the maximum production of the finished product.
4. the described method of any one according to claim 1-3, it is characterized in that, the biomass-making oilmill has method combined with it, the method is used for utilizing the flue gas (18) of steam reformer (10) and/or the heat energy of reformed gas (17), to be used for making the steam superheating (39) of using at described biomass-making oilmill, thereby drive synthetic gas turbo-driven compressor (23,24) and/or generating and improve hydrogen output (43), comprise thus the water-gas shift processing, make steam reformer (10) be connected to described pressure-variable adsorption reactor unit (42).
5. the described method of any one according to claim 1-4, it is characterized in that, described biomass-making oilmill is processed at its Fischer-Tropsch and is produced different Fischer-Tropsch tail gas in (8), namely, be sent to the processing waste gas (16) of described steam reformer (10), wherein, Fischer-Tropsch tail gas reformed (17), so that the hydrocarbon polymer of reformed gas (17) is reformed into hydrogen (43), and basically be reformatted into carbon monoxide, and further be reformatted into carbonic acid gas (44) by carbon monoxide, in described pressure-variable adsorption reactor unit (42), cool off (33) afterwards recover hydrogen (43) from gas stream, after this, residual gas (44) is recycled to steam reformer (10), to be used for that described steam reformer (10) is heated to about 800-1100 ℃ suitable temp.
6. the described method of any one according to claim 1-5, it is characterized in that, the gas (17) of reforming in described steam reformer (10) and the flue gas (18) that leaves described steam reformer (10) are sent in the heat exchanger (33) to cool off, and the heat energy of described gas stream is for making the saturated high pressure steam (26c) of leaving gasifier overheated thus.
7. the described method of any one according to claim 1-6, it is characterized in that, described heat exchanger (33) comprises superheater (33a) and (33b), wherein, make described saturated high pressure steam (26c) overheated (39) being used for compressor/turbine (24) and (23), and utilize boiler (46a) and superheater (46b) with for generation of required steam in steam reformation (10).
8. the described method of any one according to claim 1-7, it is characterized in that, vapor condensation turbine (24b) is connected to the compressor/turbine combination (23) of working as turbo-driven compressor and (24a), the low-pressure steam flow that will in the biomass-making oilmill, produce and in-high pressure steam spreads and delivers to described vapor condensation turbine, and makes generator (34) be provided for generating.
9. thereby the heat energy that utilizes the gas produce in the biomass-making oilmill makes the overheated turbine that drives described biomass-making oilmill of vapour stream and post-treatment gas stream with the application of recover hydrogen from this gas stream.
10. application according to claim 9, described application is used for utilizing the saturated steam flowing that produces at described biomass-making oilmill, wherein, the self-supporting electrobalance of crossing the biomass liquefactions heat gain and help the biomass-making oilmill as being independent of the autonomous running of independent facility of another industrial plant or electric power utility, and make simultaneously the maximum production of the finished product.
11. according to claim 9-10 described application, the steam reformer such as steam methane reformer reactor (10) that described application is combined into one for the equipment with described biomass-making oilmill, to be used for the making discharge gas stream that produces at described biomass-making oilmill overheated, thereby drive compressor and/or the generator unit of described factory, in addition, make the maximum production of the finished product of described biomass-making oilmill, thus, by means of pressure-variable adsorption reactor unit (42) recover hydrogen (43).
12. according to claim 9-11 described application, described application is used for utilizing the heat energy of flue gas (18) and/or reformed gas (17) to make the steam superheating (39) of using at described biomass-making oilmill, to be used for driving synthetic gas turbo-driven compressor (23,24) and/or to be used for generating.
13. according to claim 9-12 described application, described application is used for improving the output of described biomass-making oilmill, thus, use water-gas shift to process, steam reformer (10) and pressure-variable adsorption reactor unit (42) and the equipment of described biomass-making oilmill are combined into one.
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Application publication date: 20131030