CN105536476A - Heat recovery from a carbon dioxide capture and compression process for fuel treatment - Google Patents

Heat recovery from a carbon dioxide capture and compression process for fuel treatment Download PDF

Info

Publication number
CN105536476A
CN105536476A CN201511007835.0A CN201511007835A CN105536476A CN 105536476 A CN105536476 A CN 105536476A CN 201511007835 A CN201511007835 A CN 201511007835A CN 105536476 A CN105536476 A CN 105536476A
Authority
CN
China
Prior art keywords
gas flow
air stream
heating
air
fuel
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN201511007835.0A
Other languages
Chinese (zh)
Inventor
R.R.科特达瓦拉
J.O.巴特勒
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
General Electric Technology GmbH
Original Assignee
Alstom Technology AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Alstom Technology AG filed Critical Alstom Technology AG
Priority claimed from US12/775,541 external-priority patent/US8500891B2/en
Publication of CN105536476A publication Critical patent/CN105536476A/en
Pending legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/343—Heat recovery
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B23/00—Heating arrangements
    • F26B23/001—Heating arrangements using waste heat
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/604—Hydroxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/22—Carbon dioxide
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • 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
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • 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
    • Y02E20/32—Direct CO2 mitigation
    • 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
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Abstract

The application relates to heat recovery from a carbon dioxide capture and compression process for fuel treatment. A system and process for capturing CO<2> are disclosed. The process includes reusing heat from a CO<2> compression process by providing the heat to a fuel treatment process. The heat may used to dry a fossil fuel to improve the efficiency of the fossil fuel combustion.

Description

Reclaim heat from carbon dioxide capture and compression process to come for fuel treatment
The application be on May 7th, 2010 submit to the PCT patent application entering National Phase in China (China national application number is 201080020343.4, international application no is PCT/US2010/034016, and denomination of invention " reclaims heat from carbon dioxide capture and compression process to come for fuel treatment ") divisional application.
Technical field
The application relates generally to heat recovery.More particularly, the application relates to for reclaiming used heat and use this used heat to carry out the system and method for dry fossil fuel from carbon dioxide capture process.
Background technology
Carbon dioxide (CO 2) gas discharges into the atmosphere from the various industrial plants of such as fossil-fuelled power-plants and refuse incinerator.Although can realize significantly reducing CO by raising power conversion and utilization ratio 2discharge, but such minimizing may be not enough to the CO realizing air 2stable.Therefore, the CO catching and seal up for safekeeping the discharge of (sequestration) fossil-fuelled power-plants has been devoted to 2.
The fossil-fuelled power-plants of one type uses fine coal as Combustion Source.The water content that fine coal has can change from about 3% (weight) to about 5% (weight).In some cases, may need before producing heat, to need dry fine coal at burning pulverized coal efficiently.In these cases, operative installations steam, combustion furnace flue gas or recuperative air heater dry fine coal can be carried out.Usually, in the pulverizer of granular size reducing coal, by be used for the same air of burning pulverized coal and come dry bituminous coal or ub-bituminous coal.Such as, flue gas can flow through tubulose or recuperative air heater with heating primary air.For more rudimentary, moister coal, combustion furnace flue gas also can mix with surrounding air and supply coal supply drying unit.When using steam heat in coal drying unit, heat is supplied to fluid bed by steam, and is used as fluidizing agent and drying medium.The fossil fuel for power plant of another kind of type is brown coal, and it has high water content, and usually needs drying before combustion.
Develop various system and method to catch and recycled CO 2gas.Such as, develop by the technique based on ammonia of flue gas of WITH AMMONIA TREATMENT through cooling, the CO in ammoniacal liquor and flue gas 2react and form ammonium carbonate or carbonic hydroammonium.Can improve and the CO caught 2in conjunction with the temperature of material reverse this capture reaction, to discharge CO under stress 2.In another example, developed various amine method technology, they use the aqueous solution process flue gas of amine in the regeneration technology of absorption/stripping type, to absorb CO 2for follow-up desorb with catch.
At the CO that these are exemplary 2in catching method and in other similar approach, in order to transport and store, the CO caught 2compressed after regeneration.CO 2regeneration and compression cause there is a large amount of used heat.
Required is a kind of for being recovered in CO 2the system and method for the used heat produced in acquisition procedure, and particularly, a kind of system and method for being carried out the gross efficiency of improving device for other device or equipment operating (such as coal is dry) by recovery used heat.
The advantage be intended to of disclosed system and method meet these need in one or more or provide other favourable feature.According to this description, will make further feature and advantage apparent.Disclosed instruction extends to those embodiments fallen in the scope of claim, and no matter they whether meet in above-mentioned demand one or more.
Summary of the invention
According to each side illustrated, provide a kind of method for reclaiming heat herein.The method comprises: from air-flow, isolate a large amount of CO by acquisition procedure 2; By isolated CO 2be supplied to compression process; The heat discharged during being captured in compression process; And the heat discharged during compression process is supplied to fuel treatment process.
According to the other side illustrated herein, provide a kind of system for reclaiming heat, it comprises for isolating CO from air-flow 2capture systems and for compression from air-flow isolated CO 2compressibility, and fuel processing system.Compressibility comprise heated by compressibility at least one through heated air flow.Fuel processing system receive this at least one through heated air flow.
According to the other side illustrated, provide a kind of CO herein 2capture systems, it comprises for generation of comprising CO 2flue gas stream combustion system, for isolating a large amount of CO from flue gas stream 2capture systems, for compression from flue gas stream isolated CO 2compressibility, and fuel processing system.Compressibility comprise by compressibility heat through heated air flow.Fuel processing system receives this through heated air flow.
Above-described feature and further feature are illustrated by the following drawings and detailed description.
Accompanying drawing explanation
Fig. 1 be according to the first embodiment of the present invention in order to from CO 2acquisition procedure reclaims the schematic diagram of an embodiment of the technique of used heat.
Fig. 2 is exemplary CO 2the schematic diagram of acquisition procedure.
Fig. 3 is the schematic diagram of an embodiment according to brown coal drying process of the present invention.
Fig. 4 is the schematic diagram of another embodiment according to brown coal drying process of the present invention.
Detailed description of the invention
Fig. 1 is according to CO of the present invention 2the process chart of an exemplary embodiment of acquisition procedure 100 (hereinafter referred to as " process 100 ").With reference to Fig. 1, process 100 comprises CO 2catch or remove process 110, CO 2compression process 120, and used heat recycling process 130.In the exemplified embodiment, CO 2removing process 110 is processes based on amine.In another embodiment, CO 2remove process 110 to can be based on the process of ammonia or other process for removing acid gas contaminants from air-flow.Air-flow can be the flue gas stream from fossil fuel combustion process.
CO 2remove process 110 and comprise the CO being configured to air-flow to be clean is contacted with one or more washing lotions 2absorptive unit 201, hereinafter referred to as " absorptive unit 201 ".In one embodiment, air-flow comprises CO 2flue gas stream.In one embodiment, washing lotion can be water/amine washing lotion.In another embodiment, washing lotion can comprise amines.In one embodiment, air-flow is containing CO 2flue gas stream, and washing lotion is water/amine washing lotion.Treat therefrom to remove CO 2flue gas stream supply absorptive unit 201 by flue gas line 202.Flue gas stream is cooled by heat exchanger 203.Heat exchanger 202 provides the cooling fluid from cooling fluid feeding line 204.Cooling fluid removes heat from flue gas stream, and discharges heat exchanger by cooling fluid discharge pipe 205.
In absorptive unit 201, flue gas contacts with washing lotion.At this period of contact, the CO in flue gas 2be absorbed in washing lotion.In one embodiment, by making flue gas bubbling or washing lotion is sprayed onto the contact making flue gas and washing lotion in flue gas in washing lotion.Come absorptive unit 201 feeding wash liquid by washing lotion feeding line 220.222 extra supplementary washing lotion is supplied to absorptive unit 201 by making up line.Be stripped of CO 2flue gas leave absorptive unit 201 by discharge pipe 207.Can by heat exchanger 208 further cooling stack gas, and/or by directly contacting polishing (polish) flue gas with water in washing unit (not shown).Carry out heat exchanger 208 by pipeline 209 and cooling fluid is provided.Cooling fluid discharges heat exchanger by discharge pipe 210.
Comprise the CO of absorption 2absorptive unit 201 is left by discharge pipe 211 with the washing lotion of pollutant.Washing lotion is pumped into stripper 214 by pump 212 by heat exchanger 213, by CO in stripper 214 2separate from wash water.Gaseous state CO 2stripper 214 is left by pipeline 215.Be stripped of the CO of absorption 2regeneration washing lotion discharge stripper 214 by discharge pipe 216, and transport through heat exchanger 213, in heat exchanger 213, regenerate washing lotion from the CO comprising absorption 2washing lotion in remove heat.Then regenerate washing lotion to be cooled by heat exchanger 217.Cooling fluid is supplied from feeding line 218 heat exchanger 217.Cooling fluid discharges heat exchanger by discharge pipe 219.Then the regeneration washing lotion through cooling turns back to absorber 201 by feeding line 220 and completes absorption cycle.
CO will be left by pipeline 215 2remove the gaseous state CO of process 110 2be supplied to CO 2compression process 120.CO 2be supplied to the first flash evaporation unit 310, CO in the first flash evaporation unit 310 2cooled.CO 2the first flash evaporation unit 310 is provided in the temperature range of about 90 DEG C to about 235 DEG C.First flash evaporation unit 310 can be heat exchanger or is used as heat exchanger.The first air stream is provided to the first flash evaporation unit 310 by the first air line 309a.During the first flash process, cool CO by transferring heat to the first air stream 2.In the first flash evaporation unit 310, from CO during flash process 2in remove moisture.Moisture turns back to stripper 214 by the first moisture discharge pipe 312.In another embodiment, moisture can be supplied to there is CO 2other process of acquisition procedure 100 or system, or provide miscellaneous equipment to operate.Term " moisture " intention comprises remaining washing lotion, aqueous water, steam and their combination, and any pollutant in water and impurity.CO 2by a CO 2discharge pipe 313 is discharged from the first flash evaporation unit 308, and supplies the second flash evaporation unit 314.CO is provided to the second flash evaporation unit 314 in the temperature range of about 90 DEG C to about 235 DEG C 2.First discharges first flash evaporation unit 310 by first through heating air line 309b through heated air flow, and is supplied to blender 330.As discussed below, extra flash evaporation unit also can be heat exchanger or is used as heat exchanger.
In the second flash evaporation unit 314, from CO during the second flash process 2in remove extra moisture.From CO 2in the moisture that removes discharged from the second flash evaporation unit 314 by the second moisture discharge pipe 316, and be supplied to the second blender 335.Second air circulation is crossed the second air line 315 and is supplied to the second flash evaporation unit 314.During the second flash process in the second flash evaporation unit 314, heat is from CO 2in pass to the second air stream.Second discharges from the second flash evaporation unit 314 through heated air flow, and is supplied to blender 330 by second through heating air line 315b.CO 2by the 2nd CO 2discharge pipe 317 is discharged from the second flash evaporation unit 314, and is supplied to the first compressor unit 318.
First compressor unit 318 is by CO 2be compressed to the pressure of increase, pressurization CO 2first Heat Exchanger 380 is discharged to by the first compressor discharge pipe 319.First Heat Exchanger 380 is first intercoolers.First intercooler air circulation is crossed the first intercooler air line 380a and is supplied to the first intercooler 380.In the first intercooler 380, heat is from CO 2in pass to the first intercooler air stream.First crosses the first intercooler through the air circulation of heating intercooler discharges from the first intercooler 380 through heating air line 380b, and is supplied to blender 330.From the CO that the first intercooler 380 is discharged 2the 3rd flash evaporation unit 320 is supplied to by the first intercooler discharge pipe 319a.CO is provided to the 3rd flash evaporation unit 320 in the temperature range of about 90 DEG C to about 235 DEG C 2.
In the 3rd flash evaporation unit 320, extra moisture is by from CO 2in remove, and to be supplied in the second blender 335 by the 3rd moisture discharge pipe 322.3rd air circulation is crossed the 3rd air line 321a and is supplied to the 3rd flash evaporation unit 320.In the 3rd flash evaporation unit 320, during the 3rd flash process, heat is from CO 2in pass to the 3rd air stream.3rd discharges from the 3rd flash evaporation unit 320 through heat gas lines 321b by the 3rd through heated air flow, and is provided to blender 330.CO 2by the 3rd CO 2discharge pipe 323 is discharged from the 3rd flash evaporation unit 320, and is provided to the second compressor unit 324.
Second compressor unit 324 is by CO 2be compressed to the pressure of increase.Pressurization CO 2the second heat exchanger 382 is discharged to by the second compressor discharge pipe 325.Second heat exchanger 382 is second intercoolers.Second intercooler air circulation is crossed the second intercooler air line 331a and is supplied to the second intercooler 382.In the second intercooler 382, heat is from CO 2in pass to the second intercooler air stream.Second crosses the second intercooler through the air circulation of heating intercooler discharges from the second intercooler 382 through heating air line 331b, and is provided to blender 330.From the CO that the second intercooler 382 is discharged 2the 4th flash evaporation unit 326 is supplied to by the second intercooler discharge pipe 325b.CO is provided to the 4th flash evaporation unit 316 in the temperature range of about 90 DEG C to about 235 DEG C 2.
In the 4th flash evaporation unit 326, extra moisture is by from CO 2in remove, and be supplied to the second blender 335 by the 4th moisture discharge pipe 328.4th air circulation is crossed the 4th air line 327a and is supplied to the 4th flash evaporation unit 326.In the 4th flash evaporation unit 326, during the 4th flash process, heat is from CO 2in pass to the 4th air stream.4th discharges from the 4th flash evaporation unit 326 through heating air line 327b by the 4th through heated air flow, and is provided to blender 330.CO 2by the 4th CO 2discharge pipe 329 is discharged from the 4th flash evaporation unit 326, and can be used for further process.
As discussed the above, will respectively by first through heating air line 309b, second through heating air line 315b, 3rd through heating air line 321b and the 4th through heating air line 327b and the first intercooler through heating air line 315b and the second intercooler through heating air line 331b, will from the first flash evaporation unit 310, second flash evaporation unit 314, 3rd flash evaporation unit 320 and the 4th flash evaporation unit 326 through adding hot-air and being supplied to blender 330 from the first intercooler 380 and the second intercooler 382 through adding hot-air, and form recycling through heating air line 330b.
In another embodiment, one or more flash evaporation unit and one or more intercooler can be used to provide through adding hot-air blender 330.In another embodiment, can be combined by one or more blender and/or bypass through heating air line and/or get rid of, and form recycling through heating air line 330b.In one embodiment, first, second, third and fourth air stream and the first and second intercooler air streams are initially environment temperature to about 65 DEG C.In one embodiment, flash distillation and cooling during rolling process by air heat to the temperature between about 65 DEG C to about 180 DEG C.
In another embodiment, from air line 315,331 and 337 through add hot-air can any combination from CO 2discharge in compression process 120 and/or be supplied to blender 330.In yet another embodiment, depend on the amount of pressurization of the decrement that unit obtains and expectation, less or more flash evaporation unit 310,314,320,326 and compressor unit 318,325 can be used.
If see further in FIG such, from CO 2compression process 120 be supplied to used heat recycling process 130 through heating air line 330b from blender 330 by recycling through adding hot-air.Used heat recycling process 130 is fuel treatment processes.In the exemplified embodiment, used heat recycling process 130 is the coal crushing process with dry run.Be provided to damper 410 through adding hot-air, damper 410 can be discharged by pipeline 411 before adding hot-air bypass some through adding hot-air.This through add hot-air with from extra extra being combined through adding hot-air through heating air line 412.Extra can be provided by other source typically found at least one recuperative air heater (not shown) or power plant through adding hot-air.What at least some was extra can by the second damper 413 bypass through adding hot-air.
Through adding hot-air and extra combining in primary air pipeline 414 through adding hot-air.Primary air pipeline 414 is in fluid with air flow arrangement 415 and is communicated with, and air flow arrangement 415 controls volume and the speed of air in primary air pipeline 414.In one embodiment, this air flow arrangement 415 can be primary air (PA) fan.The flow rate through adding hot-air in primary air pipeline 414 is measured by flow measurement device 416.In one embodiment, this flow measurement device can be Pitot tube.
Pulverizer 420 being supplied to through adding hot-air, contacting with the fossil fuel being supplied to pulverizer 420 by feeding line 421 through adding hot-air in pulverizer 420.Fossil fuel can be coal fuel.In one embodiment, coal fuel can be hydrogenous coal, such as (but being not limited to) bituminous coal or ub-bituminous coal.
In pulverizer, from coal, remove moisture and/or pre-hot coal through adding hot-air.Fine coal and discharge pulverizer by dusty fuel feeding line 422 through adding hot-air.Like this, can be used to moisture-free coal from flash evaporation unit 310,314,320 and 326 through adding hot-air.Fine coal and through add hot-air be provided to boiler (not shown) for burning.In one embodiment, coal and being supplied in boiler through adding the temperature place of hot-air between about 50 DEG C and about 80 DEG C.In another embodiment, one or more pulverizer 420 can be used to process coal.
In another embodiment of the present invention, CO 2removing process 110 (Fig. 1) is the process 111 based on ammonia shown in Fig. 2.With reference to Fig. 2, the process 111 based on ammonia comprises the CO being arranged to make gas flow to be purified He washing fluid-flow contact 2absorptive unit 1101, hereinafter referred to as " absorptive unit 1101 ".Air-flow can be flue gas stream.Washing lotion stream comprises ammonia.Washing lotion stream removes and comprises CO from flue gas 2pollutant.
Treat from wherein removing CO 2flue gas supply CO by pipeline 1102 2absorptive unit 1101.Flue gas can be cooled by First Heat Exchanger 1121 before entering absorptive unit 1101.At CO 2in absorptive unit 1101, flue gas contacts with washing lotion.By making flue gas bubbling or washing lotion is sprayed onto the contact making flue gas and washing lotion in flue gas in described washing lotion.Washing lotion supplies CO by pipeline 1103 2absorptive unit.In absorptive unit 1101, by formed or in dissolved form or in the ammonium carbonate of solid form or carbonic hydroammonium by the CO in flue gas 2be absorbed in washing lotion.Through the CO comprising absorption used 2washing lotion leave absorptive unit 1101 by pipeline 1104, and be transported to steam stripping unit 1111, CO in steam stripping unit 1111 2separate from washing lotion.Isolated CO 2leave steam stripping unit by pipeline 1112, and be provided to CO 2compression process 120 (Fig. 1).Be stripped of CO 2flue gas leave absorptive unit 1101 by pipeline 1105.
The ammonia process 111 of cooling comprises washing unit 1106 further.Washing unit 1106 is configured to be stripped of CO 2dilution flue gas contact with the second wash water.Second wash water supplies washing unit 1106 by pipeline 1107.In washing unit 1106, the pollutant (such as ammonia) remained in dilution flue gas is absorbed in wash water.Wash water containing the pollutant absorbed leaves washing unit by pipeline 1108.The dilution flue gas eliminating pollutant leaves washing unit 1106 by pipeline 1109.Second wash water reclaims by regeneration unit 1110, and in regeneration unit 1110, pollutant is separated from the second wash water.In yet another embodiment, other CO can be used 2acquisition procedure comes CO 2compression process 120 provides CO 2.
In yet another embodiment of the present invention, used heat recycling process 130 (Fig. 1) is brown coal drying process.An embodiment of brown coal drying process 500 is shown in Fig. 3.With reference to Fig. 3, from CO 2compression process 120 (Fig. 1) through adding hot-air by being supplied to fluidized-bed reactor 510 through adding hot-air supply line 511.CO is received through adding hot-air supply line 511 2compression process 120 (Fig. 1) through heating air line 331.From the brown coal being supplied to fluid bed by brown coal feed line 512, moisture is removed through adding hot-air.Brown coal were roughly ground by brown coal kibbling mill 513 before being provided to fluidized-bed reactor 510, to reduce the granular size of brown coal.In another embodiment, one or more kibbling mill 513 can be used.
In fluidized-bed reactor 510, through adding hot air brown coal, and remove moisture from brown coal.From CO 2compression process through add hot-air can before being introduced into fluidized-bed reactor 510 with being combined through adding hot-air from recuperative air heater or other source.In one embodiment, fluidized-bed reactor can be supplied at the temperature place up to about 80 DEG C through adding hot-air.In another embodiment, fluidized-bed reactor 510 can be supplied to individually from independent source through adding hot-air.Like this, the present invention utilizes used heat to carry out drying brown coal or carries out supplementing drying to brown coal, operates contrary with the traditional brown coal drying using steam to carry out drying brown coal.Thus, The present invention reduces for the steam in device operation.
Wrap dampish through adding hot-air by discharge pipe 514 discharge currents fluidized bed reactor 510, and be provided to separator 515.Separator 515 can be electrostatic precipitator.At separator 515 place, any solid comprising any brown coal is separated through adding in hot-air by from bag is dampish.Solid is discharged by discharge pipe 516 and is isolated device.Wrap dampish through add hot-air by discharge pipe 517 discharge isolate device 515.Wrap and dampishly then or fluidized-bed reactor can be turned back to by pipeline 518 and fan 519 through adding hot-air, or discharged into the atmosphere by pipeline 520, or be provided to vapour condenser 521 to isolate moisture and/or steam condensing thing from the gas of being discharged by pipeline 522 further.Cooling fluid is provided by feeding line 523 and return line 524 pairs of vapour condensers 521.Cooling fluid removes heat to make humidity condensed further from bag is dampish through adding hot-air.
At fluidized-bed reactor 510 place, the brown coal removing moisture are discharged by discharge pipe 525.Then the brown coal device 526 that is cooled cools, and is provided to grinding machine 527 to reduce the granular size of brown coal further.Then dry brown coal be combined from the isolated any brown coal of deduster, and be discharged to boiler (not shown) by pipeline 530.In another embodiment, before brown coal are provided to this at least one brown coal kibbling mill 513, can use from CO 2compression process 120 (Fig. 1) from brown coal, remove moisture through adding hot-air.In this embodiment, brown coal can be contacted in second fluidized bed reactor (not shown) through adding hot-air.
Another embodiment according to brown coal drying process 500 of the present disclosure is shown in Fig. 4.As can be seen in Figure 4, drier 510a is used to carry out the fluidized-bed reactor 510 of the embodiment described in alternate figures 3.With reference to Fig. 4, from CO 2compression process 120 (Fig. 1) through adding hot-air by being supplied to drier 510a through adding hot-air supply line 511.Cycle through pipe 545 in drier 510a through adding hot-air, and do not contact brown coal.Through adding hot air brown coal, and moisture is removed by from brown coal.Moisture is removed from drier 510a by discharge pipe 514.Then what lost heat to brown coal discharges drier 510a by discharge pipe 531 through adding hot-air.Other component of Fig. 4 is identical with the description in the embodiment shown in Fig. 3.
Although illustrate and describe only some characteristic sum embodiment of the present invention, but those skilled in the art can expect many modifications and variations (such as, the use of the value of the shape of size, size, structure, each element and ratio, parameter (such as but not limited to temperature, pressure), mounting arrangements, material, pigment, directed etc. change), and do not depart from fact instruction and the advantage of the novelty of this theme described in claim.According to an alternative embodiment, any process or method step sequence or order can be changed or resequence.Therefore, should be appreciated that claims intention contains all such modifications and variations fallen in true spirit of the present invention.In addition; in order to be devoted to the concise and to the point description providing exemplary embodiment; may not describe actual realization all features (that is, do not have with the execution of current imagination optimal mode of the present invention associated those, or with make it possible to realize claimed invention do not have associated those).Should be appreciated that as develop in any engineering or design object any this actual realize time, many decisions proprietary for realization can be made.This development can be complicated and time-consuming, however, its remain benefit from those of ordinary skill of the present disclosure design, production and manufacture routine mission, and without the need to excessive test.

Claims (22)

1. the method for heating the fuel being provided to combustion system, described method comprises:
A large amount of CO is isolated from the first gas flow leaving combustion chamber 2, to provide CO 2gas flow;
Compress described CO 2gas flow, to provide the CO of compression 2gas flow;
The first air stream is utilized to carry out the CO of cooled compressed 2gas flow, with the CO of the first air stream and cooling that provide heating thus 2gas flow; And
The first air stream of heating is utilized to heat providing the described fuel to combustion system.
2. method according to claim 1, is characterized in that, the CO of cooled compressed 2gas flow comprises:
By described CO 2gas flow and described first air stream are provided to flash evaporation unit;
To described CO in described flash evaporation unit 2gas flow carries out flash distillation; And
At the CO of flash distillation 2heat exchange between gas flow and described first air stream, with the CO of the first air stream and cooling that provide heating 2gas flow.
3. method according to claim 1, is characterized in that, separation of C O from the first gas flow 2comprise:
In absorptive unit, utilize the washing lotion with absorbent to absorb CO 2, to form the CO with absorption 2washing lotion;
From the CO with absorption 2washing lotion in stripping CO 2, to provide CO 2gas flow.
4. method according to claim 3, is characterized in that, described absorbent comprises ammonium compounds.
5. method according to claim 3, is characterized in that, described absorbent comprises ammoniacal liquor.
6. method according to claim 2, is characterized in that, described flash evaporation unit is heat exchanger.
7. method according to claim 6, is characterized in that, described heat exchanger is intercooler.
8. method according to claim 1, is characterized in that, at least one that described fuel is comminuted coal or pulverizes in brown coal.
9. method according to claim 8, is characterized in that, the first air stream of heating directly heats described fuel and fluidly provides described fuel to described combustion system.
10. method according to claim 6, is characterized in that, also comprises:
The second heat exchanger is utilized to heat the second air stream, to provide the second air stream of heating;
First air stream of combined heated and the second air stream of heating; And
The first and second air streams of the heating of combination are utilized to heat described fuel.
11. methods according to claim 2, is characterized in that, cooling CO 2gas flow comprises:
CO is provided 2gas flow and the second air flow to the second flash evaporation unit;
To described CO in described second flash evaporation unit 2gas flow carries out flash distillation; And
At the CO of the second flash distillation 2heat exchange between gas flow and described second air stream, with the CO of the second air stream and cooling that provide heating 2gas flow; And
First air stream of Hybrid Heating and the second air stream of heating, to provide the heated air stream of combination for heating described fuel.
12. methods according to claim 11, is characterized in that, described second flash evaporation unit is heat exchanger.
13. 1 kinds of combustion systems, comprising:
CO 2capture systems, it has absorptive unit and steam stripping unit, to isolate a large amount of CO from the first gas flow leaving combustion chamber 2, to provide CO 2gas flow;
Compressor, for compressing described CO 2gas flow;
Heat exchanger, it is configured at described CO 2heat exchange between gas flow and the first air stream, to provide the CO of cooling thus 2first air stream of gas flow and heating; And
Fuel processing system, for preparing the fuel for described combustion system, wherein, the first air stream of heating is used for heating the fuel being provided to described combustion system.
14. combustion systems according to claim 13, is characterized in that, described heat exchanger construction is flash evaporation unit, and wherein, described CO 2gas flow flash distillation in described flash evaporation unit.
15. combustion systems according to claim 13, is characterized in that, also comprise:
Absorptive unit, for contacting described first gas flow and the washing lotion with absorbent, to absorb CO 2and form the CO with absorption 2washing lotion; And
Steam stripping unit, it is from the CO with absorption 2washing lotion in stripping CO 2, to provide CO 2gas flow.
16. combustion systems according to claim 15, is characterized in that, described absorbent comprises ammonium compounds.
17. combustion systems according to claim 15, is characterized in that, described absorbent comprises ammoniacal liquor.
18. combustion systems according to claim 13, is characterized in that, described heat exchanger is intercooler.
19. combustion systems according to claim 13, is characterized in that, at least one that described fuel is comminuted coal or pulverizes in brown coal.
20. combustion systems according to claim 19, is characterized in that, the first air stream of heating directly heats described fuel and fluidly provides described fuel to described combustion system.
21. combustion systems according to claim 14, is characterized in that, also comprise:
Second flash evaporation unit, it receives described CO 2gas flow and the second air stream, with in described second flash evaporation unit to described CO 2gas flow carries out flash distillation and at the CO of the second flash distillation 2heat exchange between gas flow and described second air stream, thus the second air stream of heating and the CO of cooling are provided 2gas flow; And
Blender, the first air stream of its combined heated and the second air stream of heating, to provide the air stream of the heating of combination for heating described fuel.
22. combustion systems according to claim 13, is characterized in that, also comprise:
Second heat exchanger, it receives described CO 2gas flow and the second air stream, with the CO in compression 2heat exchange between gas flow and described second air stream, thus the second air stream of heating and the CO of cooling are provided 2gas flow; And
Blender, the first air stream of its combined heated and the second air stream of heating, to provide the air stream of the heating of combination for heating described fuel.
CN201511007835.0A 2009-05-08 2010-05-07 Heat recovery from a carbon dioxide capture and compression process for fuel treatment Pending CN105536476A (en)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
US17673309P 2009-05-08 2009-05-08
US61/176733 2009-05-08
US12/775,541 US8500891B2 (en) 2009-05-08 2010-05-07 Waste heat recovery from a carbon capture process
CN2010800203434A CN102438731A (en) 2009-05-08 2010-05-07 Heat recovery from a carbon dioxide capture and compression process for fuel treatment
US12/775541 2010-05-07

Related Parent Applications (1)

Application Number Title Priority Date Filing Date
CN2010800203434A Division CN102438731A (en) 2009-05-08 2010-05-07 Heat recovery from a carbon dioxide capture and compression process for fuel treatment

Publications (1)

Publication Number Publication Date
CN105536476A true CN105536476A (en) 2016-05-04

Family

ID=55816322

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201511007835.0A Pending CN105536476A (en) 2009-05-08 2010-05-07 Heat recovery from a carbon dioxide capture and compression process for fuel treatment

Country Status (1)

Country Link
CN (1) CN105536476A (en)

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1900415A1 (en) * 2006-09-06 2008-03-19 Mitsubishi Heavy Industries, Ltd. CO2 recovery system and CO2 recovery method
WO2008127709A2 (en) * 2007-04-11 2008-10-23 Great River Energy Apparatus and method of enhancing the quality of high-moisture materials and separating and concentrating organic and/or non-organic material contained therein
CN101294765A (en) * 2008-06-05 2008-10-29 神华集团有限责任公司 Low rank coal high temperature flue gas drying method and device
WO2008143966A1 (en) * 2007-05-18 2008-11-27 Exxonmobil Reserch And Engineering Company Process for removing a target gas from a mixture of gases by thermal swing adsorption

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1900415A1 (en) * 2006-09-06 2008-03-19 Mitsubishi Heavy Industries, Ltd. CO2 recovery system and CO2 recovery method
WO2008127709A2 (en) * 2007-04-11 2008-10-23 Great River Energy Apparatus and method of enhancing the quality of high-moisture materials and separating and concentrating organic and/or non-organic material contained therein
WO2008143966A1 (en) * 2007-05-18 2008-11-27 Exxonmobil Reserch And Engineering Company Process for removing a target gas from a mixture of gases by thermal swing adsorption
CN101294765A (en) * 2008-06-05 2008-10-29 神华集团有限责任公司 Low rank coal high temperature flue gas drying method and device

Similar Documents

Publication Publication Date Title
CN110152489B (en) Carbon dioxide capture system and method based on steam turbine exhaust waste heat recovery
CN102438731A (en) Heat recovery from a carbon dioxide capture and compression process for fuel treatment
CN108136321B (en) For CO2Method and apparatus for trapping
EP1900415B1 (en) CO2 recovery method
WO2015176570A1 (en) Method and apparatus for high-moisture, lower heating value lignite drying and water recovery in generator set
CN103270253B (en) For being burnt and CO by carbonaceous fuel 2the method of electric power is produced in trapping
CN106268198A (en) A kind of desulfurization fume dehumidifying and water reclamation system and method
US20090158740A1 (en) Co2 capture during compressed air energy storage
CN101423214A (en) Method for catching carbon dioxide in generating plant flue gas by ammonia process and equipment thereof
CN102859304B (en) The method of driving steam turbine generating equipment and the device by brown coal generation steam
CN105536484A (en) Pollutant pretreating tower condensing based on flue gas
CN109854321B (en) Pure oxygen combustion supercritical carbon dioxide circulating power generation system and method
JP6173734B2 (en) Exhaust gas treatment system
CN111023791B (en) Drying waste heat recycling integrated device
CN104990396A (en) System for carrying out lignite drying and water recovery by using waste heat of power plant
US9157369B2 (en) Waste heat utilization for energy efficient carbon capture
CN102519299B (en) System capable of improving cooling effect of cooling tower by means of reducing moisture content of air
CN202393293U (en) Device for improving cooling effect of cooling tower by means of reducing air moisture
CN217829546U (en) Chemical method flue gas carbon dioxide entrapment system
CN105536476A (en) Heat recovery from a carbon dioxide capture and compression process for fuel treatment
CN215486191U (en) Device system for capturing energy of carbon dioxide analysis tower by amine method
CN115608133A (en) Flue gas carbon capture system and method for capturing carbon in flue gas
CN104874272A (en) Apparatus And Method For Integrating Desulfurization And Carbon Dioxide Capture
CN213480200U (en) Water-saving system for full-chain water taking of lignite machine set
CN115069066B (en) Adsorption fluidized bed carbon capture system and method utilizing low-pressure turbine steam of power plant

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
CB02 Change of applicant information

Address after: Baden, Switzerland

Applicant after: ALSTOM TECHNOLOGY LTD

Address before: Baden, Switzerland

Applicant before: Alstom Technology Ltd.

COR Change of bibliographic data
WD01 Invention patent application deemed withdrawn after publication

Application publication date: 20160504

WD01 Invention patent application deemed withdrawn after publication