CN101663376A - Unite and generate electricity and produce hydrocarbon - Google Patents

Unite and generate electricity and produce hydrocarbon Download PDF

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Publication number
CN101663376A
CN101663376A CN200880009279.2A CN200880009279A CN101663376A CN 101663376 A CN101663376 A CN 101663376A CN 200880009279 A CN200880009279 A CN 200880009279A CN 101663376 A CN101663376 A CN 101663376A
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gas
synthetic
stage
combustion gases
hydrocarbon
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CN101663376B (en
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扬·亨德里克·杜文哈格·博斯霍夫
伊莎贝拉·洛德温娜·格雷夫
安德烈·彼得·斯泰恩伯格
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Sasol Technology Pty Ltd
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Priority claimed from PCT/IB2008/050456 external-priority patent/WO2008099312A2/en
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    • 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]

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Abstract

A kind ofly be used to unite the method (10) of generating electricity and producing hydrocarbon, described method (10) comprising: in wet gasification stage (70), make gasification comprise H at least to produce 2High-pressure combustion gas (86) with CO; Make first part's enrichment (72) H of described combustion gases 2To produce rich H 2Gas (88); With second section generating (77) by described combustion gases.In dry gasification stage (16), make gasification comprise H at least to produce 2High pressure synthetic gas precursor (36) with CO.With described rich H 2At least a portion of gas (88) is mixed with described synthetic gas precursor (36) to be provided for the synthetic gas of synthetic hydrocarbon, by synthetic (20, the 22) hydrocarbon of described synthetic gas.In certain embodiments, method (10) produces CO 2Discharge stream (134) is used for other purpose to be used for chelating or collection.

Description

Unite and generate electricity and produce hydrocarbon
The present invention relates to unite and generate electricity and produce hydrocarbon.Particularly, the present invention relates to unite the method for generating electricity and producing hydrocarbon.
Coal is as the raw material of generating and generation hydrocarbon.It is generally acknowledged that integrated gasification combined cycle plants (IGCC) technology has environmental advantages than conventional burning coal-fired plant.In IGCC technology, at first gasification of coal is to produce synthetic gas, and synthetic gas is as the fuel source in combined cycle generation stage then.A kind of approach of producing hydrocarbon by coal be gasification of coal to produce synthetic gas, then synthetic gas is changed into hydrocarbon.
It will be favourable that the IGCC technology of uniting with the hydrocarbon production technique is provided, and it demonstrates economy (that is, fund and running cost) benefit and environmental benefit.
The term wet gasification stage of using in this specification sheets is meant and makes the entrained flow gasifying stage of water as the carrier of feeding-in solid body (for example coal).Therefore, with slurry feed to gasifying stage.
The term dry gasification stage of using in this specification sheets is meant the entrained flow gasifying stage of using gas as the carrier of feeding-in solid body (for example coal).
According to the present invention, a kind of method of generating electricity and producing hydrocarbon that is used to unite is provided, described method comprises:
In wet gasification stage, make gasification comprise H at least to produce 2High-pressure combustion gas with CO;
Make the enrichment H of first part of combustion gases 2To produce rich H 2Gas;
Second section generating by combustion gases;
In dry gasification stage, make gasification comprise H at least to produce 2High pressure synthetic gas precursor with CO;
With rich H 2At least a portion of gas is mixed with the synthetic gas precursor, to be provided for the synthetic gas of synthetic hydrocarbon; With
By the synthetic hydrocarbon of described synthetic gas.
Combustion gases can cling at least 45, more preferably at least 55 cling to, most preferably at least 65 cling to, for example produce under about 70 pressure that cling to.Usually, wet gasification stage makes water quenching, with cooling combusting gas.
H in the combustion gases 2Can be higher than H in the synthetic gas precursor with the mol ratio of CO 2Mol ratio with CO.For fear of ambiguity, the phrase " H that uses in this specification sheets 2Mol ratio with CO " be meant H 2Volumetric molar concentration divided by the volumetric molar concentration of CO.H 2The mol ratio of/CO has the identical meaning.
H in the combustion gases 2The mol ratio of/CO can be at least 0.6.Preferably, this mol ratio is at least 0.8, more preferably at least 0.9, for example about 0.96.Usually, H in the combustion gases 2The mol ratio of/CO is 0.6 to 1.0.
Consider the pressure-losses in the processing unit, dry gasification stage should be produced synthetic gas under sufficiently high pressure, to allow carrying out the synthetic of hydrocarbon under suitable high pressure.Usually, the pressure of synthetic gas precursor be about 40 to about 50 the crust, for example about 45 the crust.Usually, dry gasification stage comprises gasification stage waste heat boiler.
H in the synthetic gas precursor 2The mol ratio of/CO can be for about 0.3 to about 0.6, is generally about 0.3 to about 0.4, for example, and about 0.4.
The H of the first part of combustion gases 2Enrichment can comprise makes described first part carry out the aqueous vapor conversion to produce rich H 2Gas.Usually, aqueous vapor conversion is sulfur-bearing (sour) conversion, that is, contain and be suitable for making carbon monoxide and the catalyzer of water reaction with generation additional hydrogen in the presence of sulphur.
This method can comprise for example by utilizing the rich H of a film and/or pressure varying adsorption of purified part 2Gas is to produce purified basically hydrogen.Basically purified hydrogen can be used for the hydrotreatment by synthetic gas synthetic hydrocarbon.
Rich H 2Gas can be under the high pressure.The rich H of at least a portion 2Gas can comprise with mixing of synthetic gas precursor makes rich H 2Gas generates electricity by expansion turbine.
The existence that can be included in oxygen by the second section combustion gases generatings described combustion gases that burn down and under high pressure expand with the combustion gases that produce heat and the combustion gases that make described heat and to generate electricity and produce hot waste gas by the gas-turbine expander.Usually, the burning of combustion gases is carried out in burner.Hot waste gas can be under the normal atmosphere or be higher than normal atmosphere.
Can also be included in waste heat recovery stage by the generating of second section combustion gases and reclaim heat from described hot waste gas.Usually, waste heat recovery stage comprises waste heat recovery stage waste heat boiler.Usually, reclaiming heat from hot waste gas in waste heat recovery stage is included in thus and produces steam the waste heat recovery stage waste heat boiler.The steam that is produced can be used for driving steam turbine and generates electricity, and perhaps described steam can be used for other place in the technology to be used for other purpose.
Waste heat recovery stage waste heat boiler can be that cofiring burns waste heat boiler.Can produce fuel gas by the synthetic hydrocarbon of synthetic gas.Waste heat recovery stage waste heat boiler can be burnt with the fuel gas cofiring, with pressure and/or the temperature of rising by the steam of described waste heat recovery stage waste heat boiler generation.
This technology can comprise that separation of air is to produce oxygen.Oxygen can be used for making the combustion gases burning to produce the combustion gases of heat.Usually, oxygen must produce under pressure with the operating pressure in the burner that surpasses the described combustion gases of burning.Usually, the pressure with liquid oxygen pumps up and expects heats liquid oxygen then to produce oxygen, and described oxygen is used to the combustion gases that burn subsequently.
The oxygen of lower pressure also can be used for combustion fuel gas, and cofiring burns described waste heat recovery stage waste heat boiler thus.
Oxygen also is used for wet gasification stage and dry gasification stage usually so that gasification.This oxygen is the used the highest oxygen of pressure, and required pressure evaporates under pressure subsequently by the pumping liquid oxygen usually and obtains.
Can realize in the mode of any conventional by the synthetic hydrocarbon of synthetic gas.Usually, comprise that by the synthetic hydrocarbon of synthetic gas utilizing one or more Fischer-Tropsch hydrocarbon synthesis phase to carry out Fischer-Tropsch synthesizes, produce one or more and plant hydrocarbon product stream and contain CO 2, CO and H 2Fischer-Tropsch tail gas.
Described one or more Fischer-Tropsch hydrocarbon synthesis phase can be equipped with the reactor of any appropriate, for example is selected from one or more reactor in fixed-bed reactor, slurry bed reactor, ebullated bed reactor or the dry powder fluidized-bed reactor.Pressure in the reactor can for 1 the crust to 100 the crust, be usually less than 45 the crust, temperature can be 160 ℃ to 380 ℃.
One or more Fischer-Tropsch hydrocarbon synthesis phase can be for being lower than the low temperature Fischer-Tropsch hydrocarbon synthesis phase that moves under 280 ℃ the temperature.Usually, in this low temperature Fischer-Tropsch hydrocarbon synthesis phase, synthesizing under 160 ℃ to 280 ℃ temperature of hydrocarbon moves, and is preferably 220 ℃ to 260 ℃, for example is about 250 ℃.Therefore, the typical case that this low temperature Fischer-Tropsch hydrocarbon synthesis phase is high chainpropagation starches a step of reaction, and it clings to, is usually less than under the 45 predetermined running pressure that cling to 10 to 50 and moves.
One or more Fischer-Tropsch hydrocarbon synthesis phase can be the high temperature fischer-tropsch hydrocarbon synthesis phase that moves under at least 320 ℃ temperature.Usually, this high temperature fischer-tropsch hydrocarbon synthesis phase 320 ℃ to 380 ℃, for example under the about 350 ℃ temperature and at 10 to 50 crust, be usually less than under the operating pressures of 45 crust and move.This high temperature fischer-tropsch hydrocarbon synthesis phase is the low transfer reaction stage, adopts two-phase fluidised bed reactor usually.Different with the low temperature Fischer-Tropsch hydrocarbon synthesis phase that with the ability that keeps continuous liquid product phase in slurry bed reactor is feature, high temperature fischer-tropsch hydrocarbon synthesis phase can not produce successive liquid product phase in fluidized-bed reactor.
Can handle Fischer-Tropsch tail gas to remove CO 2CO 2Can remove in the mode of any conventional, for example by using benzene Fei Er (Benfield) solution to remove.Usually, Fischer-Tropsch tail gas experience aqueous vapor translate phase is to change into CO with CO 2And produce more H 2The aqueous vapor translate phase that the aqueous vapor translate phase is normally conventional does not promptly have sulphur (sweet) conversion stages.
This method can comprise separates H from Fischer-Tropsch tail gas 2(for example, using transformation absorption) also makes H 2Be circulated to one or more Fischer-Tropsch hydrocarbon synthesis phase.
This method can comprise that processing synthetic gas precursor or synthetic gas are to remove desulfuration and/or CO 2Handling synthetic gas precursor or synthetic gas can realize in any conventional mode, for example, utilizes the low-temp methanol washing process (Rectisol process) that comprises the low-temp methanol washing to realize.
This method can comprise the CO by processing synthetic gas precursor or synthetic gas and/or the acquisition of processing Fischer-Tropsch tail gas 2A part be fed to the burner that is used for by second section combustion gases generatings, with as temperature regulato.Usually, this comprises compression CO 2To surpass the operating pressure of burner.The CO of compression 2Can before being fed to burner, mix with the oxygen that has pressurizeed.
This method can comprise that processing mainly comprises CO from waste heat recovery stage waste heat boiler 2With the waste gas of water, anhydrate and stay CO to remove 2Discharge stream, this CO 2Discharge stream can any conventional mode chelating (sequestrated), perhaps collect and be used for other purpose.CO 2Discharge stream can with handle from synthetic gas precursor or synthetic gas and/or Fischer-Tropsch tail gas is handled another part CO that obtains 2Merge.Scheme or additionally, this method can comprise part waste gas or the portion C O that makes from waste heat recovery stage waste heat boiler instead 2Discharge stream is circulated to burner.
This method can comprise utilizes fuel gas and air to make steam superheating from waste heat recovery stage waste heat boiler.In this case, by make stack gas that steam superheating produces not should with mix from the waste gas of waste heat recovery stage waste heat boiler or from the hot waste gas of gas turbine expander.
This method can be included in hydrocarbon and produce the purified basically oxygen of use or purified basically oxygen and CO at least some relevant combustion equipment 2Mixture replace air.Then can be in conjunction with stack gas, so that produce CO from this class combustion equipment 2Stream merge.
Now with reference to accompanying schematic figure the present invention is described by way of example, in the accompanying drawing:
Fig. 1 shows according to of the present invention and is used to unite the technology of generating electricity and producing hydrocarbon; With
Fig. 2 illustrates in greater detail the part of the technology of Fig. 1.
With reference to Fig. 1, Reference numeral 10 is often referred to according to the technology of generating electricity and producing hydrocarbon of uniting of the present invention.Technology 10 comprises common coal system oil (CTL) hydrocarbon synthesis device and common integrated gasification combined cycle plants (IGCC) equipment of representing with Reference numeral 12 of representing with Reference numeral 14.
CTL equipment 12 comprises dry gasification stage 16, gas clean-up stage 18, the first Fischer-Tropsch hydrocarbon synthesis phase 20, with the first Fischer-Tropsch hydrocarbon synthesis phase, the 20 placed in-line second Fischer-Tropsch hydrocarbon synthesis phases 22, hjeavu ends recovery stage 24, water-gas or do not have sulphur translate phase 26, CO 2The treatment stage of removal stage 28, hydrogen separation phase 30, reaction water treatment stage 32 and product 34.
Synthetic gas pipeline 36 leads to gas clean-up stage 18 from dry gasification stage 16, then from gas clean-up stage 18 through the first Fischer-Tropsch hydrocarbon synthesis phase 20 and the second Fischer-Tropsch hydrocarbon synthesis phase 22.Fischer-Tropsch tail gas pipeline 38 leads to hjeavu ends recovery stage 24 from the second Fischer-Tropsch hydrocarbon synthesis phase 22, leads to aqueous vapor or does not have sulphur translate phase 26, CO from it then 2The removal stage 28, and finally lead to hydrogen separation phase 30.Hydrogen circulation line 40 turns back to the first Fischer-Tropsch hydrocarbon synthesis phase 20 from hydrogen separation phase 30, and fuel gas pipe 42 leads to IGCC equipment 14 from hydrocarbon separation phase 30.
44 bypasses of synthetic gas by-pass line are by the first Fischer-Tropsch hydrocarbon synthesis phase 20.
Sulphur recovery line 46 and CO 2Pipeline 48 is derived from gas clean-up stage 18.
Hydrocarbon product pipeline 50 and reaction water line 52 derive from the first Fischer-Tropsch hydrocarbon synthesis phase 20 and the second Fischer-Tropsch hydrocarbon synthesis phase 22, and wherein reaction water line 52 is led to reaction water treatment stage 32, the treatment stage that hydrocarbon product pipeline 50 leading to product 34.The treatment stage of product 34 also by lead to product the treatment stage from hjeavu ends recovery stage 24 34 light hydrocarbons line 54 be connected to hjeavu ends recovery stage 24.
Oxygenation property management line 56 and water pipeline 58 are derived from reaction water treatment stage 32, and LPG pipeline 60, petroleum naphtha pipeline 62 and diesel oil pipeline 64 34 are derived from product the treatment stage.
CO 2The removal stage 28 is equipped with CO 2Pipeline 66.
IGCC equipment 14 comprises wet gasification stage 70, sulfur-bearing translate phase 72, hydrogen-rich gas expansion stages 74, gas clean-up stage 76, combustion gases expansion stages 77, gaseous combustion and expansion stages 78 and comprises that cofiring burns the waste heat recovery stage 80 of waste heat boiler 82 and steam turbine 84.
Combustion gas line 86 is led to gas clean-up stage 76 from wet gasification stage 70, leads to the combustion gases expansion stages 77 from gas clean-up stage 76 then, and leads to thus gaseous combustion and expansion stages 78.Combustion gas line 86 between wet gasification stage 70 and the gas clean-up stage 76 is gone back branch road and is communicated to sulfur-bearing translate phase 72.Rich H 2Gas tube 88 passes the hydrogen-rich gas expansion stages 74 and is connected with the dry gasification stage 16 of CTL equipment 12 and the synthetic gas pipeline 36 between the gas clean-up stage 18 from sulfur-bearing translate phase 72.
Removal of sulphur pipeline 90 is derived from gas clean-up stage 76.
With reference to accompanying drawing 2, gaseous combustion and expansion stages 78 comprise compressor 92 and drive the gas turbine expander 94 that is connected to compressor 92.Combustion gas line 86 from the combustion gases expansion stages 77 is led to burner 96.CO 2 Pipeline 98 feeds in the compressor 92.The CO of compression 2Pipeline 102 leads to burner 96 and is connected with oxygen pipeline 100 from compressor 92.The combustion gas line 104 of heat is led to gas turbine expander 94 from burner 96.The cofiring that hot exhaust gas line 106 is led to waste heat recovery stage 80 from gas turbine expander 94 burns waste heat boiler 82.
Vapour line 108 burns waste heat boiler 82 from cofiring and leads to steam turbine 84, and condensation product circulation line 110 leads to cofiring from steam turbine 84 and burns waste heat boiler 82.Cofiring burns waste heat boiler 82 and is connected with fuel gas pipeline 42 from CTL equipment 12, and is equipped with waste line 112.
Hydrogen-rich gas expansion stages 74, combustion gases expansion stages 77, gaseous combustion and expansion stages 78 and steam turbine 84 provide electric power, and electric power is represented with Reference numeral 114 usually.Can output power or inner the use, for example be used for CTL equipment 12.
CTL equipment 12 and IGCC equipment 14 common air tripping devices 120, CO 2With water sepn stage 122, CO 2Compression and water sepn stage 124 and water treatment stage 126.
Oxygen pipeline 100 from air separation plant 120 leads to gaseous combustion and expansion stages 78, as mentioned before, uses oxygen equipment but also lead in CTL equipment 12 and the IGCC equipment 14 other.
CO from the gas clean-up stage 18 of CTL equipment 12 2 Pipeline 48 leads to CO 2With water sepn stage 122, CO 2Pipeline 98 is from CO 2Lead to gaseous combustion and the compressor of expansion stages 78 92 with the water sepn stage 122.Water pipeline 128 is from CO 2Lead to water treatment stage 126 with the water sepn stage 122.
CO 2Compression and water sepn stage 124 and from the waste line 112 of waste heat recovery stage 80 with from the CO of CTL equipment 12 2The CO in removal stage 28 2 Pipeline 66 links to each other.
Water pipeline 130 is from CO 2Compression and water sepn stage 124 are led to water treatment stage 126, and described water treatment stage 126 also is connected with water pipeline 58 from the reaction water treatment stage 32 of CTL equipment 12.One or more treated water lines 132 (for one only is shown for simplicity) is led to CTL equipment 12 and IGCC equipment 14 from water treatment stage 126.
Refer again to accompanying drawing 2, air separation plant 120 is equipped with air feed pipeline 134 and nitrogen production flow line 136.
Paniculate coal gasifies in dry gasification stage 16 to produce the synthetic gas precursor.Dry gasification stage 16 can adopt the dry gasification technology of any conventional, for example produces H 2/ CO mol ratio is Shell (trade(brand)name) the entrained flow dryer feed gasification technology of about 0.4 synthetic gas precursor.Although not shown in the diagram, be to use waste heat boiler to cool off the synthetic gas precursor that under the pressure of about 45 crust, produces usually.Waste heat boiler produces the process steam (not shown).The synthetic gas precursor is fed to gas clean-up stage 18 by synthetic gas pipeline 36.Yet the synthetic gas precursor is at first by making rich H 2Gas is along rich H 2Gas tube 88 flows and enriched hydrogen increases H thus 2/ CO mol ratio is so that H 2/ CO mol ratio is about 0.7 to about 2.5.
In gas clean-up stage 18, purify synthetic gas in the mode of any conventional, to remove desulfuration, particulate material and CO 2Can use conventional purified synthesis gas technology, for example the CO of benzene Fei Er solution is washed and adopted to low-temp methanol washing process, amine 2Absorption technique.Sulphur is removed from gas clean-up stage 18 by sulphur recovery line 46, CO 2Pass through CO 2Pipeline 48 is removed.
The synthetic gas that purifies is fed to the first Fischer-Tropsch hydrocarbon synthesis phase 20, and is fed to the second Fischer-Tropsch hydrocarbon synthesis phase 22 thus, so that synthetic gas is changed into hydrocarbon.Can use the synthetic configuration of Fischer-Tropsch hydrocarbon of any conventional.In the embodiment shown in the accompanying drawing 1, show the two-stage process that adopts synthetic gas bypass (using synthetic gas by-pass line 44) and hydrogen circulation (utilizing hydrogen circulation line 40).Therefore, Fischer-Tropsch hydrocarbon synthesis phase 20,22 can comprise the reactor that one or more is suitable, for example fluidized-bed reactor, tubular fixed bed reactor, slurry bed reactor or ebullated bed reactor.It in addition can be included in a plurality of reactors that move under the different condition.Pressure in the reactor can for 1 the crust to 100 the crust, but use in this embodiment about 45 the crust pressure.Temperature can be 160 ℃ to 380 ℃.Therefore, reactor will comprise the fischer-tropsch catalysts of particle form.Catalyzer can comprise Co, Fe, Ni, Ru, Re and/or Rh as its active catalyst composition, but preferably contains Fe as its active catalyst composition.Catalyzer can have one or more kind promotors that are selected from basic metal, V, Cr, Pt, Pd, La, Re, Rh, Ru, Th, Mn, Cu, Mg, K, Na, Ca, Ba, Zn and Zr.Catalyzer can be the catalyzer of load, and in the catalyzer of load, for example the active catalyst composition of Co is carried on for example Al of suitable carriers 2O 3, TiO 2, SiO 2, in ZnO or its combination.Preferably, catalyzer is the Fe catalyzer of not load.
In the first Fischer-Tropsch hydrocarbon synthesis phase 20 and the second Fischer-Tropsch hydrocarbon synthesis phase 22, produce reaction water, this reaction water removes and is fed to reaction water treatment stage 32 by reaction water line 52.In reaction water treatment stage 32, utilize conventional isolation technique with oxygenation thing and reaction water from, and remove by oxygenation property management line 56.Water is fed to water treatment stage 126 from reaction water treatment stage 32 extractions and by water pipeline 58.
The hydrocarbon product that produces in the first Fischer-Tropsch hydrocarbon synthesis phase 20 and the second Fischer-Tropsch hydrocarbon synthesis phase 22 is removed by hydrocarbon product pipeline 50 and be fed to product the treatment stage 34.The treatment stage of product in 34, hydrocarbon product to be producing LPG gas, petroleum naphtha and diesel oil, and described LPG gas, petroleum naphtha and diesel oil 34 are removed from product the treatment stage by LPG pipeline 60, petroleum naphtha pipeline 62 and diesel oil pipeline 64 respectively.
Fischer-Tropsch tail gas is removed from the second Fischer-Tropsch hydrocarbon synthesis phase 22 by Fischer-Tropsch tail gas pipeline 38, and is fed to hjeavu ends recovery stage 24, locates for example C of light hydrocarbon at this 3 +Hydrocarbon is removed in a usual manner, and 34 handles with 34 hydrocarbon product with enter product by hydrocarbon product pipeline 50 treatment stage be fed to product by light hydrocarbons line 54 treatment stage.Then, Fischer-Tropsch tail gas is mixed with the steam (not shown), and carries out known water-gas shift reaction so that CO and water (steam) are changed into CO in no sulphur translate phase 26 2And H 2Contain the CO that concentration increases this moment 2And H 2Fischer-Tropsch tail gas be fed to CO from no sulphur translate phase 26 2The removal stage 28.At CO 2In the removal stage 28, reuse routine techniques and come from Fischer-Tropsch tail gas, to remove CO 2And water.Usually, this comprises use benzene Fei Er solution absorption CO 2Then, desorption CO again 2, and pass through CO 2Pipeline 66 is from CO 2The removal stage 28 is removed CO 2Be fed to CO with water and with it 2Compression and water sepn stage 124.
The CO that concentration reduces will be contained this moment 2With the Fischer-Tropsch tail gas of water from CO 2The removal stage 28 is fed to hydrocarbon separation phase 30.In hydrocarbon separation phase 30, use conventional transformation absorption from the Fischer-Tropsch tail gas separation of hydrogen, produce the fuel gas that mainly comprises CO and appropriate hydrocarbon gas.Hydrogen is circulated to the first Fischer-Tropsch hydrocarbon synthesis phase 20 by hydrogen circulation line 40.Fuel gas removes and is fed to the waste heat recovery stage 80 of IGCC equipment 14 by fuel gas pipeline 42.Randomly, fuel gas can be used as synthetic natural gas and sells, and can mix with other air-flow to obtain correct specification for sale.
In order to generate electricity, in the wet gasification stage 70 of IGCC equipment 14, make the coal slurry gasification to produce combustion gases.Can use the wet gasification technology of any conventional, for example General Electric (trade(brand)name) slurry feed gasification technology.Make water as the coal carrier, make coal slurry gasify, thereby in wet gasification stage 70, produce H 2/ CO mol ratio is about 0.96 combustion gases.The common water quenching of combustion gases cools off.Combustion gases produce under the pressure that is higher than 70 crust.
Gas clean-up stage 76 is removed and be fed to combustion gases from wet gasification stage 70 by combustion gas line 86.Before gas clean-up stage 76, partial combustion gas mixes with the steam (not shown) as required and is transferred to sulfur-bearing translate phase 72, and wherein CO and water conservancy change into CO with known water-gas shift reaction 2And H 2In sulfur-bearing translate phase 72, produce rich H thus 2Gas, and described rich H 2Gas is by rich H 2Gas tube 88 is fed to hydrogen expansion stage 74.In hydrogen expansion stage 74, rich H 2Gas expansion is by expansion turbine, and it drives generator, with generating.In expansion turbine, rich H 2The pressure of gas is reduced to about 45 crust, rich then H from being higher than 70 crust 2Gas mixes with synthetic gas precursor in the synthetic gas pipeline 36, to increase the H of synthetic gas precursor 2/ CO mol ratio, as mentioned before.
In gas clean-up stage 76, combustion gases purify in a usual manner to remove desulfuration along removal of sulphur pipeline 90.Then, via the combustion gases expansion stages 77 combustion gases that purify are fed to gaseous combustion and expansion stages 78 by combustion gas line 86.In the combustion gases expansion stages 77, the combustion gases of purification expand by gas turbine expander, the pressure of combustion gases is reduced to the operating pressure of gaseous combustion and expansion stages 78, and generates electricity (representing with Reference numeral 114 usually).
In air separation plant 120, utilize conventional Cryogenic air separation technology separation of air, to produce nitrogen and oxygen, as more being shown specifically among Fig. 2.Nitrogen is removed by nitrogen pipeline 136 and be used for CTL equipment 12 and IGCC equipment 14 under the situation of needs, perhaps reclaims to be used for commercial purpose or purging is gone out.Oxygen from air separation plant 120 is removed by oxygen pipeline 100, and also is assigned in CTL equipment 12 and the IGCC equipment 14 to use under the situation of needs.Partial oxygen is fed to gaseous combustion and the burner of expansion stages 78 96 (see figure 2)s by oxygen pipeline 100.
At CO 2In the water sepn stage 122, water is from CO 2In isolate.Water is fed to water treatment stage 126 by water pipeline 128.CO 2From CO 2Remove and be fed to gaseous combustion and the compressor of expansion stages 78 92 with the water sepn stage 122.
Thus with CO 2CO in the pipeline 98 2Be fed to compressor 92 and compression.Compressed CO 2Mix with hyperbaric oxygen from oxygen pipeline 100, and compressed CO 2Pass through compressed CO with the oxygen mixture 2Be fed to burner 96 with oxygen pipeline 102.Combustion gases by combustion gas line 86 chargings are at CO 2With burning in burner 96 under the existence of oxygen, to produce the combustion gases of heat.The logical superheated of the combustion gases of heat combustion gas line 104 is removed and is passed through gas turbine expander 94, and it is by direct mechanical connection drive compression machine 92.Gas turbine expander 94 also is used to drive the generator (not shown) to produce electric power, and electric power is represented with Reference numeral 114 usually.Mainly comprise CO 2From gas turbine expander 94, remove by hot exhaust gas line 106 with the hot waste gas of water, and be fed to the cofiring burning waste heat boiler 82 of waste heat recovery stage 80.Waste heat boiler 82 utilizes by the fuel gas of fuel gas pipeline 42 chargings and produces high pressure steam, described high pressure steam is fed to steam turbine 84 by vapour line 108, steam turbine 84 is used to drive the generator (not shown), to produce electric power, electric power is represented with Reference numeral 114 usually.Condensation product is circulated to cofiring from steam turbine 84 and burns waste heat boiler 82.
Gas turbine expander 94 and/or steam turbine 84 can combine with air separation plant 120, to drive the air compressor of air separation plant 120 by direct mechanical connection.
In cofiring burnt waste heat boiler 82, the waste gas that is produced by the burning of fuel gas combined with the waste gas from gas turbine expander 94, and removes by waste line 112.Should be understood that this waste gas mainly comprises CO 2And water.Waste gas is fed to CO 2Compression and water sepn stage 124, and with its compression.Water is from compressed CO 2Separate and be fed to water treatment stage 126 by water pipeline 130.From CO 2The compressed CO in compression and water sepn stage 124 2Can be used for chelating or collection, shown in Reference numeral 134.Therefore, compressed CO 2For example can be used for enhanced recovery of oil (EOR) or enhanced coalbed methane and reclaim (ECBMR).
In water treatment stage 126, will be fed to the water treatment of water treatment stage 126 to the level that needs along water pipeline 58,128 and 130.CTL equipment 12 and IGCC equipment 14 are removed and be dispensed to treated water by treated water pipeline 132, and therein as boiler feed water.
The gasification technology of selecting to be suitable for particular case most will be considered multiple factor, comprises the intended use of feedstock characteristic, fund cost, running cost, reliability, the synthetic gas of producing etc.As shown in the figure, the invention provides a kind of IGCC power generation assembly and CTL device of associating, the described IGCC power generation assembly and the CTL device that carry out of uniting has benefited from the optimum macro economy of fund-intensive part, and CO is provided 2Chelating.The combination of dry gasification and wet gasification is used to provide the intermediate flow that is suitable for synthetic hydrocarbon and generating respectively.For generating, but advantageously wet gasification process supply pressure is higher than 70 combustion gases that cling to.The synthetic gas precursor of (about usually 45 crust) but dry gasification process supply pressure and Fischer-Tropsch hydrocarbon synthetic need be complementary.Combustion gases have the hydrogen richness than height before the synthetic gas usually, and a part of combustion gases are provided for the suitable charging of enriched hydrogen thus, more than are mixed into the H of gas precursor 2With the CO mol ratio.In addition, wet gasification stage adopts water quick cooling usually, thus combustion gases under high relatively temperature by water saturation.Advantageously, reduced the steam demand of the sulfur-bearing conversion that is used to make first part's combustion gases enriched hydrogen thus.In addition, dry gasification stage adopts the waste heat boiler that process steam is provided usually.Because it is more effective that the dry gasification method is rich in aspect the synthetic gas of carbon monoxide and the required process steam in production, and wet gasification technology is the method for the most effective production hydrogen-rich gas, imitates so the combination of dry gasification technology and wet gasification technology has improved total energy.
Advantageously, the size that can suitably adjust IGCC equipment to be only being used for inner energy consumption, or scheme as an alternative, if near have suitable electrity market, the size of IGCC equipment can be adjusted into the economical efficiency of scale maximization that makes electric power output.
Because big compression needs, air separation plant is built expensive and the operation power consumption.Advantageously, when IGCC equipment and the CTL equipment common air tripping device, the economical efficiency of scale has reduced the cost of the required per unit volume oxygen of CTL equipment.The power generation turbine of IGCC equipment can be integrated by the air compressor of direct mechanical connection and air separation plant, improves the efficiency of device thus, and its reason is a loss in efficiency of having avoided relevant with generating.
Facility shared reduced and has been used for the cost of supplement boiler water inlet with the expensive ultrapure water of the steam producing IGCC equipment steam turbine and use.Because better the economical efficiency of scale can also realize saving aspect the use cost that is used for the CTL device.
Can be used as for example fuel in the heat reclamation device of IGCC equipment of IGCC equipment by the fuel gas (being blown away in many cases) of CTL device fabrication.This allows to produce the steam that pressure is higher and/or temperature is higher.Owing to fuel gas shifts from large-scale equipment is inner, so cost will reduce.From the angle of CTL equipment, this fuel gas stream that is chosen as provides inner reliable user.
Be used for the electric power that the CTL device interior consumes with optimum cost and benefit production, compare, improved the CTL of associating and the total carbon efficiencies and the plant efficiency of IGCC equipment with two kinds of equipment that separate.
At last, the permission of uniting of CTL equipment and IGCC equipment is collected CO from the waste gas of IGCC equipment 2This portion C O by producing in the CTL equipment 2The compressor that imports the gas turbine expander of IGCC equipment with the pure oxygen from air separation plant is realized, avoids thus nitrogen is introduced in the burner of IGCC equipment.This allows gas turbine to utilize oxygen and CO 2Oxygen and the N of mixing when replace using air 2Conventional mixture work.Therefore, the final waste gas from IGCC equipment will be purified relatively CO 2With the combination of water vapour, its can with the residue CO that produces by CTL equipment 2In conjunction with being used for output, make CO 2The economical efficiency of scale that processing and gas booster compressor have benefited from increasing.

Claims (12)

1. unite the method for generating electricity and producing hydrocarbon for one kind, described method comprises:
In wet gasification stage, make gasification comprise H at least to produce 2High-pressure combustion gas with CO;
Make the enrichment H of first part of described combustion gases 2To produce rich H 2Gas;
Second section generating by described combustion gases;
In dry gasification stage, make gasification comprise H at least to produce 2High pressure synthetic gas precursor with CO;
With described rich H 2At least a portion in the gas is mixed with described synthetic gas precursor to be provided for the synthetic gas of synthetic hydrocarbon; With
By the synthetic hydrocarbon of described synthetic gas.
2. the described method of claim 1, H in the wherein said combustion gases 2Be higher than H in the described synthetic gas precursor with the mol ratio of CO 2Mol ratio with CO.
3. claim 1 or 2 described methods, H in the wherein said combustion gases 2The mol ratio of/CO is at least 0.6.
4. each described method in the aforementioned claim, H in the wherein said synthetic gas precursor 2The mol ratio of/CO is about 0.3 to about 0.6.
5. each described method in the aforementioned claim, it comprises the described rich H of purifying 2Part in the gas is to produce purified basically hydrogen.
6. each described method in the aforementioned claim, wherein said rich H 2Gas is in high pressure, and wherein with described rich H 2At least a portion of gas is mixed with described synthetic gas precursor and is comprised and make described rich H 2Gas by expansion turbine with the generating.
7. each described method in the aforementioned claim, wherein the existence that is included in oxygen by the generating of the second section of the described combustion gases described combustion gases that burn down and under high pressure expand with generating with the combustion gases that produce heat and the combustion gases that make described heat by the gas-turbine expander and produce hot waste gas, and reclaim hot from described hot waste gas in the waste heat recovery stage that comprises the waste heat boiler that produces steam.
8. the described method of claim 7, wherein said waste heat boiler is that cofiring burns waste heat boiler, and wherein produce fuel gas, burn described waste heat boiler, with the pressure and/or the temperature of rising by the steam of described waste heat boiler generation with described fuel gas cofiring by the synthetic hydrocarbon of described synthetic gas.
9. each described method in the aforementioned claim wherein comprises that by the synthetic hydrocarbon of described synthetic gas the Fischer-Tropsch that uses one or more Fischer-Tropsch hydrocarbon synthesis phase is synthetic, produces one or more and plants hydrocarbon product stream and contain CO 2, CO and H 2Fischer-Tropsch tail gas.
10. the described method of claim 9 is wherein handled described Fischer-Tropsch tail gas to remove CO 2, and/or wherein handle described synthetic gas precursor or described synthetic gas to remove CO 2, the CO that obtains from the processing of the processing of described synthetic gas precursor or synthetic gas and/or described Fischer-Tropsch tail gas 2A part be fed to the burner that is used for by the generating of the second section of described combustion gases, with as temperature regulato.
11. the described method of claim 7, it comprises that processing mainly comprises CO from described waste heat boiler 2Anhydrate to remove with the waste gas of water, stay CO 2Discharge stream, described CO 2Discharge stream is chelated or collects and is used for other purpose.
12. each described method in the aforementioned claim, wherein said wet gasification stage makes water quenching cool off described combustion gases.
CN200880009279.2A 2007-02-12 2008-02-08 Co-production of power and hydrocarbons Expired - Fee Related CN101663376B (en)

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102627981A (en) * 2011-02-07 2012-08-08 通用电气公司 Energy recovery in syngas applications
CN106662013A (en) * 2014-08-11 2017-05-10 三菱日立电力系统株式会社 Integrated gasification combined cycle power generation facility and method for operating integrated gasification combined cycle power generation facility
CN108026790A (en) * 2015-09-24 2018-05-11 三菱重工业株式会社 Waste heat recovery plant, internal-combustion engine system and ship and waste recovery method
CN109596663A (en) * 2018-11-23 2019-04-09 太原理工大学 A kind of CO2The method for being enriched with the coal instant heating gasification, and combustion under hyperbaric environment

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4199327A (en) * 1978-10-30 1980-04-22 Kaiser Engineers, Inc. Process for gasification of coal to maximize coal utilization and minimize quantity and ecological impact of waste products
US4341069A (en) * 1980-04-02 1982-07-27 Mobil Oil Corporation Method for generating power upon demand
DE3415224A1 (en) * 1984-04-21 1985-10-24 Kraftwerk Union AG, 4330 Mülheim GAS TURBINE AND STEAM POWER PLANT WITH AN INTEGRATED COAL GASIFICATION PLANT
GB2237814A (en) * 1989-11-10 1991-05-15 Shell Int Research A method and apparatus for co-generating power and hydrocarbons from coal derived synthesis gas using pressure swing absorption
CN1125866C (en) * 2000-03-03 2003-10-29 石油大学(北京) Process for synthesizing liquid hydrocarbon with natural gas and its synthesizing catalyst
CN100378194C (en) * 2005-12-22 2008-04-02 上海兖矿能源科技研发有限公司 Method of coproducing oil products and electric energy using synthetic gas as raw material

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CN102627981A (en) * 2011-02-07 2012-08-08 通用电气公司 Energy recovery in syngas applications
US8992640B2 (en) 2011-02-07 2015-03-31 General Electric Company Energy recovery in syngas applications
CN102627981B (en) * 2011-02-07 2016-08-03 通用电气公司 Energy regenerating in synthesis gas application
CN106662013A (en) * 2014-08-11 2017-05-10 三菱日立电力系统株式会社 Integrated gasification combined cycle power generation facility and method for operating integrated gasification combined cycle power generation facility
CN106662013B (en) * 2014-08-11 2018-07-27 三菱日立电力系统株式会社 The operation method of gasifying combined generating apparatus and gasifying combined generating apparatus
CN108026790A (en) * 2015-09-24 2018-05-11 三菱重工业株式会社 Waste heat recovery plant, internal-combustion engine system and ship and waste recovery method
CN109596663A (en) * 2018-11-23 2019-04-09 太原理工大学 A kind of CO2The method for being enriched with the coal instant heating gasification, and combustion under hyperbaric environment

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ZA200906031B (en) 2010-04-28

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