CN102343201A - Process for removing acid gas from flue gas by using residual heat of flue gas - Google Patents
Process for removing acid gas from flue gas by using residual heat of flue gas Download PDFInfo
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- CN102343201A CN102343201A CN2011103061323A CN201110306132A CN102343201A CN 102343201 A CN102343201 A CN 102343201A CN 2011103061323 A CN2011103061323 A CN 2011103061323A CN 201110306132 A CN201110306132 A CN 201110306132A CN 102343201 A CN102343201 A CN 102343201A
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- flue gas
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- heat exchanger
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 119
- 239000003546 flue gas Substances 0.000 title claims abstract description 119
- 238000000034 method Methods 0.000 title claims abstract description 32
- 239000007789 gas Substances 0.000 title claims abstract description 15
- 239000002253 acid Substances 0.000 title claims abstract description 9
- 238000010521 absorption reaction Methods 0.000 claims abstract description 173
- 239000007788 liquid Substances 0.000 claims abstract description 73
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 56
- 238000010438 heat treatment Methods 0.000 claims abstract description 25
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims abstract description 18
- 229910017604 nitric acid Inorganic materials 0.000 claims abstract description 18
- 239000002918 waste heat Substances 0.000 claims abstract description 15
- 238000011069 regeneration method Methods 0.000 claims abstract description 8
- 230000008929 regeneration Effects 0.000 claims abstract description 6
- 238000001816 cooling Methods 0.000 claims abstract 2
- 238000006477 desulfuration reaction Methods 0.000 claims description 59
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 54
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 39
- 241000282326 Felis catus Species 0.000 claims description 31
- 238000005516 engineering process Methods 0.000 claims description 24
- 239000000047 product Substances 0.000 claims description 22
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 19
- 238000005057 refrigeration Methods 0.000 claims description 19
- 230000023556 desulfurization Effects 0.000 claims description 18
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 15
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 13
- 239000000920 calcium hydroxide Substances 0.000 claims description 13
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 13
- 239000000243 solution Substances 0.000 claims description 13
- 239000003507 refrigerant Substances 0.000 claims description 10
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 9
- 239000005864 Sulphur Substances 0.000 claims description 9
- 238000004519 manufacturing process Methods 0.000 claims description 9
- 239000011259 mixed solution Substances 0.000 claims description 9
- 150000001412 amines Chemical class 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 8
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 claims description 8
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical group NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 claims description 7
- GSEJCLTVZPLZKY-UHFFFAOYSA-N Triethanolamine Chemical compound OCCN(CCO)CCO GSEJCLTVZPLZKY-UHFFFAOYSA-N 0.000 claims description 7
- 238000007600 charging Methods 0.000 claims description 7
- 238000005261 decarburization Methods 0.000 claims description 7
- 239000004615 ingredient Substances 0.000 claims description 7
- 239000007791 liquid phase Substances 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 7
- 239000007790 solid phase Substances 0.000 claims description 7
- 229940043237 diethanolamine Drugs 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 6
- 239000006096 absorbing agent Substances 0.000 claims description 4
- 238000005262 decarbonization Methods 0.000 claims description 4
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 claims description 4
- 239000000428 dust Substances 0.000 claims description 4
- 230000003009 desulfurizing effect Effects 0.000 claims description 3
- 230000002441 reversible effect Effects 0.000 claims description 3
- 239000000779 smoke Substances 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 2
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 239000012467 final product Substances 0.000 claims description 2
- -1 monomethyl diethanol amine Chemical compound 0.000 claims description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 2
- 238000009418 renovation Methods 0.000 claims description 2
- 239000012071 phase Substances 0.000 claims 2
- 238000005191 phase separation Methods 0.000 claims 1
- 238000004064 recycling Methods 0.000 claims 1
- 238000000638 solvent extraction Methods 0.000 abstract 1
- 239000012267 brine Substances 0.000 description 12
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 12
- 239000003245 coal Substances 0.000 description 9
- 239000000463 material Substances 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 230000002378 acidificating effect Effects 0.000 description 6
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 6
- 230000006835 compression Effects 0.000 description 5
- 238000007906 compression Methods 0.000 description 5
- 238000007599 discharging Methods 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 230000000630 rising effect Effects 0.000 description 5
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 229910000027 potassium carbonate Inorganic materials 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000003916 acid precipitation Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- 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
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- 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
-
- 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
- B01D53/75—Multi-step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
-
- 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
- B01D53/14—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 by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing 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
- Y02C20/10—Capture or disposal of greenhouse gases of nitrous oxide (N2O)
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a process for removing acid gas from flue gas by using residual heat of the flue gas. The process comprises the following steps of: introducing flue gas into a heat exchanger I; lowering the temperature of the flue gas; making the flue gas enter a desulfurizing-absorbing tower; heating and gasifying water in the tube pass of the heat exchanger and making the heated and gasified water enter a phase splitter; combining the heat exchanger and the phase splitter into a waste heat boiler, wherein the generated steam pressure is 3-6 Pa; partitioning the water steam into three streams for entering a low-pressure steam turbine I, a low-pressure steam turbine II and a heater respectively; driving the low-pressure steam turbine I with the water steam for supplying a power source to a refrigerator to obtain chilled water, wherein the chilled water is taken as cooling media of the desulfurizing-absorbing tower, a denitrifing-absorbing tower and CO2 absorbing tower respectively to keep the temperatures of the towers at respective needed temperatures; driving the low-pressure steam turbine II with the second stream of water steam; compressing desulfurized flue gas; making the desulfurized flue gas enter the denitrifing-absorbing tower to remove NOx and generate dilute nitric acid simultaneously; and supplying a heat source to a CO2 regeneration tower through a heater H1 by using the third stream of water steam to regenerate a CO2 absorption liquid, using the water steam circularly, and generating and collecting CO2 simultaneously.
Description
Technical field
The present invention relates to a kind of technology of utilizing the flue gas waste heat to remove its sour gas.
Background technology
China is that a few is one of country of main energy sources with coal in the world, is maximum in the world coal production state and country of consumption.Coal still accounts for significant proportion in the energy resource structure of China, China is that main energy consumption structure is the most important reason that causes that China's atmosphere pollution is on the rise with coal.According to statistics, China's 90% sulfur dioxide, 67% nitrogen oxide, 70% smoke discharge amount come from the burning of coal.Wherein, smoke emissioning pollution problems such as coal fired power plant, coal-burned industrial boiler, coal-fired furnace kiln are the most outstanding.With 2001-2010 was sample in these 10 years, the generated energy that China is annual, and the coal electricity has accounted for about 75%.Along with the industrialization paces of China are accelerated, power consumption also constantly increases, and the coal that need be used to generate electricity is also just more and more, and the discharging of the flue gas that causes thus increases the weight of the pollution of atmosphere is also corresponding day by day.With 1,000,000 kilowatts of coal-fired power plants is example, and its SO2 emissions are 2.6 ten thousand tons of every year, and nitrogen oxide emission is 1.4 ten thousand tons of every year, and CO2 emissions are 6,000,000 tons of every year.And carbon dioxide is the main matter that causes greenhouse effects in the flue gas of coal-fired power plant's discharging, SO
2, NOx is again the main source that causes atmosphere pollution such as acid rain and photochemical fog.How eliminating these pollutions is problem demanding prompt solutions.And the flue gas that coal-fired power plant discharges contains certain waste heat, and directly the wherein latent heat of flood tide has been wasted in discharging, does not meet requirements of saving energy.To above situation, the present invention proposes a kind of new technology of utilizing the flue gas waste heat to remove its contained sour gas, and this technology can make full use of the waste heat in the flue gas, can remove oxysulfide, nitrogen oxide and CO in the flue gas again
2, make flue gas reach discharge standard, meet the requirement of energy-saving and emission-reduction.The acidic materials wherein of partially recycled utilization simultaneously obtain nitric acid product and CO
2Be used for a plurality of fields such as chemical industry and modern agriculture as raw material, thus the creation of value.
Summary of the invention
The purpose of this invention is to provide a kind of new technology of utilizing the flue gas waste heat to remove himself contained sour gas; Mainly remove oxysulfide, nitrogen oxide and carbon dioxide; Make flue gas emissions reach corresponding national standards, and reclaim wherein useful chemical resource.
For realizing above-mentioned target, technical scheme of the present invention is following:
A kind of technology of utilizing the flue gas waste heat to remove its sour gas, it is made up of desulphurization system, denitrating system and decarbonization system.Its flow process as shown in Figure 1, it may further comprise the steps:
(1) flue gas is at first passed through electric dust collector; Remove the most of dust in the flue gas; Again flue gas is passed among the heat exchanger I E1 through pipeline 2; Water is walked tube side; Flue is made shell side leave with rage; Through after the heat exchange; The temperature of flue gas reduces; Get into desulfuration absorbing tower T1; And the water in the tube side is heated among the vaporization back entering phase-splitter V1; Water after the phase-splitting turns back among the heat exchanger I E1; Heat exchanger E1 and phase-splitter V1 combine and are equivalent to a waste heat boiler; The steam pressure that produces is 3 ~ 6 atmospheric pressure, and water vapour is divided into three stocks through current divider I S1 and does not get into low-pressure turbine I TU1 and low-pressure turbine II TU2 and heater H 1, water vapour driving low-pressure turbine I TU1; This T Steam Turbine U1 is as the power source of refrigeration machine C1; Make refrigeration machine C1 refrigeration, thereby obtain chilled water (brine ice etc.), brine ice then is sent to cooler I C2 respectively through current divider II S2; Cooler II C3 and cooler III C4 are as desulfuration absorbing tower T1; Denitration absorption tower T2 and CO
2The refrigerant of absorption tower T3 makes desulfuration absorbing tower T1, denitration absorption tower T2 and CO
2Absorption tower T3 temperature remains on required separately temperature respectively; Second strand of water vapour is used to drive low-pressure turbine II TU2; This steam turbine II TU2 is as the power source of compressor CO1; Make compressor CO1 acting, and compression makes its pressure brought up to more than the 0.25MPa by pressure-fired from the flue gas of desulfuration absorbing tower T1 cat head discharge; And entering denitration absorption tower T2; To remove NOx, produce rare nitric acid simultaneously, the 3rd strand of steam is CO through heater H 1
2Regenerator T4 provide thermal source, with regeneration CO
2Absorption liquid recycles;
(2) flue gas through heat exchanger I E1 heat exchange gets into desulfuration absorbing tower T1 bottom; Fully contact with sulphur absorption liquid (being generally the mixed solution of calcium hydroxide and NaOH) from 3 chargings of desulfuration absorbing tower T1 top duct; Flue gas after the desulfurization is discharged from desulfuration absorbing tower T1 top; Mixing back (amount of entrained air is determined by Chemical Calculation according to the amount of contained NO the flue gas) with the air that gets into from pipeline 12 gets into by among the steam turbine II TU2 compressor driven CO1; Make the pressure of gas be increased to the above back of 0.25MPa from bottom entering denitration absorption tower T2; The sulphur absorption liquid then drops to tower bottom along desulfurizing tower; Remove solid phase through Separation of Solid and Liquid, liquid phase can return the doctor solution liquid pool and recycle;
(3) after flue gas and the AIR MIXTURES after the pressurization got into denitration absorption tower T2, with NOx absorption liquid (the being generally water) counter current contacting that pipeline 5 through T2 top, denitration absorption tower gets into, the discharge of T2 cat head got into CO again from the denitration absorption tower
2Absorption tower T3, and the absorption liquid (rare nitric acid) that descends from top to bottom along denitrating tower gets at the bottom of the denitration Tata, and be delivered to nitric acid product storage tank through pipeline 6;
(4) flue gas after the denitration gets into CO from the bottom
2Absorption tower T3, CO
2Absorption liquid generally adopts hot potassium carbonate solution or organic amine, the CO in the flue gas
2After in decarbonizing tower T3, being absorbed, discharge through pipeline 7 from cat head, at this moment the acid ingredient in the flue gas all is removed basically, and wherein, SOx and NOx can be controlled in 50ml/m respectively
3And 30ml/m
3Below, CO
2Then can be lower than 5000ml/m
3Below, from CO
2The CO that absorption tower T3 descends from top to bottom
2Absorption liquid gets into CO after then delivering to heat exchanger II E2 heat exchange through column bottoms pump
2Regenerator T4 top;
(5) at CO
2CO among the regenerator T4
2Again separated sucking-off, get into bulking system from cat head through piping 11, the pressurization can obtains CO
2The manufacturing other products is sold or be used as to product, the CO after the regeneration
2Absorption liquid gets into decarburization absorption tower T3 through blender M2 and recycles CO after returning heat exchanger II E2 heat exchange through pump III P3 at the bottom of the T4 tower
2The heat that regenerator T4 needs is obtained by the steam heater via H1 that phase-splitter V1 provides; And returning blender M1 through pump I P1, the liquid that condensation is got off recycles; The refrigerant of cooler I C2, cooler II C3 and cooler III C4 outlet then freezes to refrigerant refrigeration machine C1 through pump P2 blowback once more, recycles.
Can utilize the thermal source in the flue gas continuously through above five steps is oxysulfide, nitrogen oxide and the CO that removes wherein
2The required energy (comprising heat energy, pressure ability and cold energy) is provided, and makes flue gas reach discharge standard.It is pointed out that above step carries out continuously, under steady working condition, five steps are carried out simultaneously, and organically combine, and are not intermittently operated, and the present invention just just is divided into five steps for convenience and narrates.
Calculate through the whole process energy balance, for the flue gas more than 300 ℃, contained energy is higher than this process far away and removes the required gross energy of acidic materials (being about more than 2 times) in the flue gas.Therefore, the loss of Considering Energy transfer process and the influence of efficiency of utilization, as long as flow process and equipment design and type selecting is appropriate, this process removes the energy of acidic materials fully can be self-sufficient.
The above-mentioned technology that removes its sour gas; The removal methods of described oxysulfide selects the mixed solution (calcium hydroxide and NaOH mass fraction are that 10-40%, calcium hydroxide and NaOH mass ratio are 4:1 in the solution) of calcium hydroxide and NaOH as absorption liquid; It is more than 120 ℃ that flue gas advances to absorb the Tata temperature, and the oxysulfide removal efficiency is more than 90%.
The above-mentioned technology that removes its sour gas, the removal methods of described nitrogen oxide select to use empty G&W as absorption liquid, and temperature remains on 5 ~ 30 ℃.Contain the flue gas of NOx and the ratio of air and confirm that method is following: 1 volume NO consumes the O of 0.75 volume
2, 1 volume NO
2Consume the O of 0.25 volume
2, contain the O of 0.2 volume in 1 volumes of air
2According to NO, NO in the flue gas
2Content, ratio and flow, calculate the theoretical air flow, actual air flow is 1.5 ~ 2:1 with the ratio of theoretical air flow, thereby draws the amount of required actual air.
The above-mentioned technology that removes its sour gas, described CO
2Removal methods generally adopt hot potassium carbonate (composition be K
2CO
3, mass fraction is that 30% o'clock assimilation effect is best) and solution, maybe can adopt organic amine (to use ripe monoethanolamine (MEA) in the industry.Diethanol amine (DEA), triethanolamine (TEA) or N monomethyl diethanol amine (MDEA)) as absorption liquid; Absorption reaction is reversible reaction; Temperature need remain on required separately temperature; Organic amine remains on 20 ~ 40 ℃ as the absorption liquid temperature, and the hot potassium carbonate solution temperature need remain on 95 ~ 105 ℃.
The above-mentioned technology that removes its sour gas, described CO
2Renovation process select to use Steam Heating, make temperature remain on about 110 ℃ and get final product.Its principle is to absorb CO
2The material that forms of absorption liquid raise or during low pressure, react reverse carrying out at solution temperature, both can emit CO
2, solution can obtain regeneration again.
Whether the above-mentioned technology that removes its sour gas according to nitrogen-containing oxide whether in the flue gas, needs the denitrification step of denitration absorption tower T2 in the decision technology.
The new technology of utilizing the flue gas waste heat to remove its sour gas of the present invention has following some superior part:
(1) the present invention is directed to that flue gas contains a large amount of oxysulfides, nitrogen oxide and CO in the present coal electricity project
2Deng pollutant, like direct discharging, can cause serious pollution, desulfurization at present, denitration and decarburization and CO to environment
2Regeneration is very ripe technically; But because desulfurization, denitration and decarbonization system needs is just can carry out under the cryogenic high pressure situation; Especially obtain high pressure system and need the additive decrementation energy; Desulfurization in addition, denitration and decarbonization device adopt the absorption liquid absorption process; Because absorption process is a strong exothermic process; If at the untimely transfer liberated heat of each absorber portion, assimilation effect will be undesirable.Compressor CO1, cooler C1, C2, C3, C4, heater H 1 all needs the additional energy input.And flue gas self contains certain waste heat, and directly discharging does not meet requirements of saving energy.The present invention is directed to this situation, the water vapour after obtaining heating through heat exchanger E1 and phase-splitter V1 is compressor CO1, cooler C1, C2, C3, C4, and heater H 1 provides energy source.New technology not only makes full use of the waste heat in the flue gas, can remove oxysulfide, nitrogen oxide and CO in the flue gas again
2And collection CO wherein
2, make the discharge standard that reaches of flue gas, and need not extra energy input, meet the requirement of energy-saving and emission-reduction.
(2) desulfurization in the document, denitration, decarburization and CO
2Regeneration research separately is a lot, and integrated technique is studied seldom.The present invention makes desulphurization system-denitrating system-CO
2Absorption system-CO
2Regenerative system organically is coupled, and makes desulfurization, denitration, decarburization and the CO of flue gas
2It is integrated to regenerate.In actual use, can be according to nitrogen oxide, oxysulfide and CO in the flue gas
2Content need to confirm desulfurization, denitration, decarburization and CO
2One or more of regenerating unit.
(3) this patent is not merely to removing the acidic materials in the flue gas, but the acidic materials resource that removes, partially recycled utilization acidic materials wherein obtain nitric acid product and CO
2Be used for a plurality of fields such as chemical industry and modern agriculture as raw material, thus the creation of value.
Description of drawings
Fig. 1 removes the production technology of its sour gas and the process flow diagram of device for a kind of flue gas waste heat that utilizes of the present invention, and wherein: T1 is a desulfuration absorbing tower; T2 is the denitration absorption tower; T3 is CO
2The absorption tower; T4 is CO
2Regenerator; E1 is the heat exchanger I; E2 is the heat exchanger II; C1 is a refrigerator; C2 is the cooler I; C3 is the cooler II; C4 is the cooler III; TU1 is the low-pressure turbine I; TU2 is the low-pressure turbine II; CO1 is a compressor; P1 is the pump I; P2 is the pump II; P3 is the pump III, M1, M2; M3, M4 are blender, and S1, S2 are current divider; H1 is a heater, and 1 for replenishing the fresh water feed pipe, and 2 is the flue gas feed pipe; 3 are desulfurization absorption liquid feed pipe, and 4 is the sulfuric acid discharge pipe, and 5 is the denitration absorbing liquor feed pipe; 6 is the nitric acid discharge pipe, and 7 is the flue gas discharge line after desulphurization denitration and the decarburization, and 8 is the aqueous water feed pipe; 9,10 be respectively the denitration absorbing liquor of adding and the absorption liquid feed pipe that desorber returns, 11 is CO
2Conduit, 12 is air duct.
The specific embodiment
Through embodiment the present invention is specifically described below, but can not be interpreted as restriction scope of patent protection of the present invention.
Embodiment 1:
Handle flue gas, in volume fraction, it contains CO at present
2Be 13.98%, O
2Be 3.49%, N
2Be 72.87%, SO
2Be 0.21%, H
2O is 9.45%, and exhaust gas volumn is 1124980 m
3/ h, flue-gas temperature is 300 ℃.Can know by above-mentioned content, because nonnitrogenous oxide wherein contains SO
2And CO
2Sour gas needs desulfuration absorbing tower T1 and CO
2Absorption tower T3 and CO
2Regenerator T4 need not denitration absorption tower T2.Flue gas gets into heat exchanger E1 through pipeline 2, makes the temperature of flue gas reduce to 120 ℃ by 300 ℃, adds hot water simultaneously, and the steam that obtains and the mixture of aqueous water get into phase-splitter V1, and water returns heat exchanger E1 recirculation after the phase-splitting.Steam is divided into two strands through current divider S1, and one is CO as heating source through heater H 1
2Regenerator T4 heating makes that desorber T4 temperature is 110 ℃.Another burst entering low-pressure turbine I TU1 is converted into mechanical energy to heat energy, makes refrigeration machine C1 refrigeration, thereby obtains brine ice, and brine ice then makes desulfurizing tower T1 keep 120 ℃ of constant temperature through cooler C2, makes CO through cooler C4
2The absorption tower keeps 25 ℃ of constant temperature, prevents that the temperature rising is unfavorable for the absorption of oxysulfide and oxycarbide.The flue gas that cools down through heat exchanger I E1 gets into desulfuration absorbing tower T1; Desulfuration absorbing tower T1 adopts packed tower; 9.9 meters of tower diameters; 59.5 meters of tower heights, utilize the solute mass fraction be the mixed solution of 20% calcium hydroxide and NaOH as absorption liquid, through pipeline 3 from the cat head charging; Its flow is 18585; Absorb back sulphur absorption liquid and drop to tower bottom along desulfuration absorbing tower T1, remove solid phase through Separation of Solid and Liquid, liquid phase can return the doctor solution liquid pool and recycle.Flue gas after the desulfurization gets into CO
2Absorption tower T3.CO
2Absorption tower T3 adopts packed tower, and diameter is 9.8 meters, and tower height is 49 meters, and monoethanolamine (MEA) gets into CO as absorption liquid through pipeline 9
2Absorption tower T3, its flow do, the flue gas after the absorption enters atmosphere after pipeline 7 gets into chimneys, because the acid ingredient in this moment flue gas all is removed allow compliance with emission standards basically.From CO
2The CO that absorption tower T3 descends from top to bottom
2Absorption liquid gets into CO after then delivering to the E2 heat exchange through column bottoms pump
2Regenerator T4 top.Utilize the part steam among the phase-splitter V1 that the thermal source heating is provided, 4.3 meters of desorber T4 tower diameters, temperature remains on about 110 ℃ in 21.5 meters of the tower heights, tower.At CO
2CO among the regenerator T4
2Again separated sucking-off, flow is 286235kgh
-1, getting into bulking system from cat head through pipeline 11, the pressurization can obtains CO
2The manufacturing other products is sold or be used as to product.Monoethanolamine at the bottom of the tower (MEA) is back to CO through pump P3
2Absorption tower T3 recycles.
Embodiment 2:
Handle flue gas, in volume fraction, it contains CO at present
2Be 7.6%, O
2Be 10%, N
2Be 54%, H
2O is 28%, and every cubic metre contains SO
3Quality is 1500 mg, contains NO
XBeing mainly NO, is 1200 mg, and exhaust gas volumn is 12000 m
3/ h, flue-gas temperature is 300 ℃.Can know by above-mentioned content, owing to wherein contain nitrogen oxide, SO
2And CO
2Sour gas needs desulfuration absorbing tower T1, denitrating tower to absorb T2, CO
2Absorption tower T3 and CO
2Regenerator T4.Earlier flue gas is passed through heat exchanger E1; Make the temperature of flue gas reduce to 120 ℃ by 300 ℃; Be heated behind the water process heat exchanger E1 of blender M1 from pipeline 1 simultaneously; Water after the heating and steam mixture get into phase-splitter V1, return heat exchanger E1 through the aqueous water after the phase-splitting through blender M1 and recycle.Water vapour after the phase-splitting is divided into three strands through current divider S1, and one is CO as heating source through heater H 1
2Regenerator T4 heating, second gang of entering low-pressure turbine I TU1, this steam turbine I TU1 make refrigeration machine C1 refrigeration, thereby obtain chilled water (brine ice etc.) as the power source of refrigeration machine C1.Brine ice then is sent to cooler I C2, cooler II C3 and cooler III C4 respectively as desulfuration absorbing tower T1, denitration absorption tower T2 and CO through current divider S2
2The refrigerant of absorption tower T3 makes desulfuration absorbing tower T1, denitration absorption tower T2 and CO
2Absorption tower T3 temperature keeps 120 ℃, 20 ℃ and 25 ℃ respectively, prevents that the temperature rising is unfavorable for oxysulfide, nitrogen oxide and CO
2Absorption.The 3rd strand of water vapour is through low-pressure turbine II TU2; This T Steam Turbine U2 make compressor CO1 acting, and compression is from the flue gas of desulfuration absorbing tower T1 cat head discharge as the power source of compressor CO1; Its pressure is brought up to more than the 0.25MPa by pressure-fired, and got into denitration absorption tower T2.
The flue gas that cools down through heat exchanger E1 gets into desulfuration absorbing tower T1; Adopt packed tower; Its tower diameter is 1 meter; Tower height is 7 meters, utilize the solute mass fraction be the mixed solution of 10% calcium hydroxide and NaOH as absorption liquid, through pipeline 3 from the cat head charging; Its flow is 85; Absorb back sulphur absorption liquid and drop to tower bottom along desulfuration absorbing tower T1, remove solid phase through Separation of Solid and Liquid, liquid phase can return the doctor solution liquid pool and recycle.Flue gas after the desulfurization and the flow that feeds from pipeline 12 are that 66 air mixes, get into compressor CO1 pressurization back entering denitration absorption tower T2.Denitration absorption tower T2 adopts packed tower, and tower diameter is 0.9 meter, 5 meters of tower heights.Pipeline 5 through cat head feeds NOx absorption liquid water.The absorption liquid (rare nitric acid) that descends from top to bottom along denitrating tower gets at the bottom of the T2 tower of denitration absorption tower, and is delivered to nitric acid product storage tank through pipeline 6.The T2 cat head comes out and the flue gas after out of stock is from the denitration absorption tower, gets into CO
2Absorption tower T3.CO
2Absorption tower T3 adopts packed tower, and 1.1 meters of tower diameters are high 5.5 meters.Diethanol amine (DEA) gets into CO from pipeline 9 through blender M2 as absorption liquid
2Absorption tower T3, flow does.Fully the flue gas after the contact is discharged from chimney through piping 7 after from cat head, because the acid ingredient in the flue gas all is removed allow compliance with emission standards basically at this moment.Absorb CO
2The organic amine absorption liquid from CO
2Absorption tower T3 gets into CO through heat exchanger II E2 heating back
2Regenerator T4 utilizes the part Steam Heating of phase-splitter V1, makes temperature remain on about 115 ℃, is to get into bulking system from the pipeline of cat head 11 with the flow after the desorb, and the pressurization can obtains CO
2The manufacturing other products is sold or be used as to product.After diethanol amine at the bottom of the tower (DEA) the process pump P3 process heat exchanger II E2 heat exchange, M2 is back to CO through blender
2Absorption tower T3 recycles.
Embodiment 3:
Handle flue gas, in volume fraction, it contains CO at present
2Be 12.06%, O
2Be 10.1%, N
2Be 60.54%, SO
2Be 0.12%, NOx is 0.1%, H
2O is 17.08%, and exhaust gas volumn is 1442650 m
3/ h, flue-gas temperature is 415 ℃.Can know by above-mentioned content, owing to wherein contain nitrogen oxide, SO
2And CO
2Sour gas needs desulfuration absorbing tower T1, denitration absorption tower T2, CO
2Absorption tower T3 and CO
2Regenerator T4.Earlier flue gas is passed through heat exchanger I E1; Make the temperature of flue gas reduce to 120 ℃ by 415 ℃; Be heated behind the water process heat exchanger E1 of blender M1 from pipeline 1 simultaneously; Water after the heating and steam mixture get into phase-splitter V1, return heat exchanger I E1 through the aqueous water after the phase-splitting through blender M1 and recycle.Water vapour after the phase-splitting is divided into three strands through current divider S1, and one is CO as heating source through heater H 1
2Regenerator T4 heating, second gang of entering low-pressure turbine I TU1, this steam turbine I TU1 make refrigeration machine C1 refrigeration, thereby obtain chilled water (brine ice etc.) as the power source of refrigeration machine C1.Brine ice then is sent to cooler I C2, cooler II C3 and cooler III C4 respectively as desulfuration absorbing tower T1, denitration absorption tower T2 and CO through current divider S2
2The refrigerant of absorption tower T3 makes desulfuration absorbing tower T1, denitration absorption tower T2 and CO
2Absorption tower T3 temperature keeps 130 ℃, 30 ℃ and 40 ℃ respectively, prevents that the temperature rising is unfavorable for oxysulfide, nitrogen oxide and CO
2Absorption.The 3rd strand of water vapour is through low-pressure turbine II TU2; This steam turbine II TU2 make compressor CO1 acting, and compression is from the flue gas of desulfuration absorbing tower T1 cat head discharge as the power source of compressor CO1; Its pressure is brought up to more than the 0.25MPa by pressure-fired, and got into denitration absorption tower T2.
The flue gas that cools down through heat exchanger I E1 gets into desulfuration absorbing tower T1; Desulfuration absorbing tower T1 adopts packed tower; 11.29 meters of tower diameters; 60 meters of tower heights, utilize the solute mass fraction be the mixed solution of 40% calcium hydroxide and NaOH as absorption liquid, through pipeline 3 from the cat head charging; Its flow is 13618; Absorb back sulphur absorption liquid and drop to tower bottom along desulfuration absorbing tower T1, remove solid phase through Separation of Solid and Liquid, liquid phase can return the doctor solution liquid pool and recycle.Flue gas after the desulfurization and the flow that feeds from pipeline 12 are that 5500 air mixes, get into compressor CO1 pressurization back entering denitration absorption tower T2.Denitrating tower T2 adopts packed tower, and tower diameter is 10.97 meters, 48 meters of tower heights.Pipeline 5 through cat head feeds NOx absorption liquid water.The absorption liquid (rare nitric acid) that descends from top to bottom along denitration absorption tower T2 gets at the bottom of the T2 tower of denitration absorption tower, and is delivered to nitric acid product storage tank through pipeline 6.The T2 cat head comes out and the flue gas after out of stock is from the denitration absorption tower, gets into CO
2Absorption tower T3.
Flue gas after the denitration gets into CO
2Absorption tower T3.CO
2Absorption tower T3 adopts packed tower, and diameter is 9 meters, and tower height is 38 meters, and triethanolamine (TEA) gets into CO as absorption liquid through pipeline 9
2Absorption tower T3, its flow do, the flue gas after the absorption enters atmosphere after pipeline 7 gets into chimneys, because the acid ingredient in this moment flue gas all is removed allow compliance with emission standards basically.From CO
2The CO that absorption tower T3 descends from top to bottom
2Absorption liquid gets into CO after then delivering to heat exchanger II E2 heat exchange through column bottoms pump
2Regenerator T4 top.Utilize the part steam in the phase-splitter that the thermal source heating is provided, 4 meters of desorber T4 tower diameters, temperature remains on about 115 ℃ in 19 meters of the tower heights, tower.At CO
2CO among the regenerator T4
2Again separated sucking-off, flow is that through pipeline 11 entering bulking systems, the pressurization can obtains CO from cat head
2The manufacturing other products is sold or be used as to product.Triethanolamine at the bottom of the tower (TEA) is back to CO through pump P3
2Absorption tower T3 recycles.
Embodiment 4:
Handle flue gas, in volume fraction, it contains CO at present
2Be 12.06%, O
2Be 10.1%, N
2Be 60.54%, SO
2Be 0.12%, NOx is 0.1%, H
2O is 17.08%, and exhaust gas volumn is 1442650 m
3/ h, flue-gas temperature is 360 ℃.Can know by above-mentioned content, owing to wherein contain nitrogen oxide, SO
2And CO
2Sour gas needs desulfuration absorbing tower T1, denitration absorption tower T2, CO
2Absorption tower T3 and CO
2Regenerator T4.Earlier flue gas is passed through heat exchanger I E1; Make the temperature of flue gas reduce to 120 ℃ by 360 ℃; Be heated behind the water process heat exchanger I E1 of blender M1 from pipeline 1 simultaneously; Water after the heating and steam mixture get into phase-splitter V1, return heat exchanger E1 through the aqueous water after the phase-splitting through blender M1 and recycle.Water vapour after the phase-splitting is divided into three strands through current divider S1, and one is CO as heating source through heater H 1
2Regenerator T4 heating, second gang of entering low-pressure turbine I TU1, this steam turbine I TU1 make refrigeration machine C1 refrigeration, thereby obtain chilled water (brine ice etc.) as the power source of refrigeration machine C1.Brine ice then is sent to cooler I C2, cooler II C3 and cooler III C4 respectively as desulfuration absorbing tower T1, denitration absorption tower T2 and CO through current divider S2
2The refrigerant of absorption tower T3 makes desulfuration absorbing tower T1, denitration absorption tower T2 and CO
2Absorption tower T3 temperature keeps 120 ℃, 25 ℃ and 95 ℃ respectively, prevents that the temperature rising is unfavorable for oxysulfide, nitrogen oxide and CO
2Absorption.The 3rd strand of water vapour is through low-pressure turbine II TU2; This T Steam Turbine U2 make compressor CO1 acting, and compression is from the flue gas of desulfuration absorbing tower T1 cat head discharge as the power source of compressor CO1; Its pressure is brought up to more than the 0.25MPa by pressure-fired, and got into denitration absorption tower T2.
The flue gas that cools down through heat exchanger I E1 gets into desulfuration absorbing tower T1; Desulfuration absorbing tower T1 adopts packed tower; 11.29 meters of tower diameters; 60 meters of tower heights, utilize the solute mass fraction be the mixed solution of 30% calcium hydroxide and NaOH as absorption liquid, through pipeline 3 from the cat head charging; Its flow is 13618; Absorb back sulphur absorption liquid and drop to tower bottom along desulfuration absorbing tower T1, remove solid phase through Separation of Solid and Liquid, liquid phase can return the doctor solution liquid pool and recycle.Flue gas after the desulfurization and the flow that feeds from pipeline 12 are that 5500 air mixes, get into compressor CO1 pressurization back entering denitration absorption tower T2.Denitration absorption tower T2 adopts packed tower, and tower diameter is 10.97 meters, 48 meters of tower heights.Pipeline 5 through cat head feeds NOx absorption liquid water.The absorption liquid (rare nitric acid) that descends from top to bottom along the denitration absorption tower gets at the bottom of the denitration Tata, and is delivered to nitric acid product storage tank through pipeline 6.The T2 cat head comes out and the flue gas after out of stock is from the denitration absorption tower, gets into CO
2Absorption tower T3.
Flue gas after the denitration gets into CO
2Absorption tower T3.CO
2Absorption tower T3 adopts packed tower, and diameter is 10 meters, and tower height is 48 meters, and hot potassium carbonate gets into CO as absorption liquid through pipeline 9
2Absorption tower T3, its flow do, the flue gas after the absorption enters atmosphere after pipeline 7 gets into chimneys, because the acid ingredient in this moment flue gas all is removed allow compliance with emission standards basically.From CO
2The CO that absorption tower T3 descends from top to bottom
2Absorption liquid gets into CO after then delivering to heat exchanger II E2 heat exchange through column bottoms pump
2Regenerator T4 top.Utilize the part steam in the phase-splitter that the thermal source heating is provided, 4 meters of desorber T4 tower diameters, temperature remains on about 120 ℃ in 19 meters of the tower heights, tower.At CO
2CO among the regenerator T4
2Again separated sucking-off, flow is that through pipeline 11 entering bulking systems, the pressurization can obtains CO from cat head
2The manufacturing other products is sold or be used as to product.Hot potassium carbonate solution at the bottom of the tower is back to CO through pump P3
2Absorption tower T3 recycles.
Embodiment 5:
Handle flue gas, in volume fraction, it contains CO at present
2Be 7.6%, O
2Be 10%, N
2Be 54%, H
2O is 28%, and every cubic metre contains SO
3Quality is 1500 mg, contains NO
XBeing mainly NO, is 1200 mg, and exhaust gas volumn is 12000 m
3/ h, flue-gas temperature is 415 ℃.Can know by above-mentioned content, owing to wherein contain nitrogen oxide, SO
2And CO
2Sour gas needs desulfuration absorbing tower T1, denitration absorption tower T2, CO
2Absorption tower T3 and CO
2Regenerator T4.Earlier flue gas is passed through heat exchanger I E1; Make the temperature of flue gas reduce to 120 ℃ by 415 ℃; Be heated behind the water process heat exchanger I E1 of blender M1 from pipeline 1 simultaneously; Water after the heating and steam mixture get into phase-splitter V1, return heat exchanger I E1 through the aqueous water after the phase-splitting through blender M1 and recycle.Water vapour after the phase-splitting is divided into three strands through current divider S1, and one is CO as heating source through heater H 1
2Regenerator T4 heating, second gang of entering low-pressure turbine I TU1, this T Steam Turbine U1 make refrigeration machine C1 refrigeration, thereby obtain chilled water (brine ice etc.) as the power source of refrigeration machine C1.Brine ice then is sent to cooler I C2, cooler II C3 and cooler III C4 respectively as desulfuration absorbing tower T1, denitration absorption tower T2 and CO through current divider S2
2The refrigerant of absorption tower T3 makes desulfuration absorbing tower T1, denitration absorption tower T2 and CO
2Absorption tower T3 temperature keeps 130 ℃, 30 ℃ and 105 ℃ respectively, prevents that the temperature rising is unfavorable for oxysulfide, nitrogen oxide and CO
2Absorption.The 3rd strand of water vapour is through low-pressure turbine II TU2; This T Steam Turbine U2 make compressor CO1 acting, and compression is from the flue gas of desulfuration absorbing tower T1 cat head discharge as the power source of compressor CO1; Its pressure is brought up to more than the 0.25MPa by pressure-fired, and got into denitration absorption tower T2.
The flue gas that cools down through heat exchanger I E1 gets into desulfuration absorbing tower T1; Adopt packed tower; Its tower diameter is 1 meter; Tower height is 7 meters, utilize the solute mass fraction be the mixed solution of 20% calcium hydroxide and NaOH as absorption liquid, through pipeline 3 from the cat head charging; Its flow is 85; Absorb back sulphur absorption liquid and drop to tower bottom along desulfuration absorbing tower T1, remove solid phase through Separation of Solid and Liquid, liquid phase can return the doctor solution liquid pool and recycle.Flue gas after the desulfurization and the flow that feeds from pipeline 12 are that 66 air mixes, get into compressor CO1 pressurization back entering denitration absorption tower T2.Denitration absorption tower T2 adopts packed tower, and tower diameter is 0.9 meter, 5 meters of tower heights.Pipeline 5 through cat head feeds NOx absorption liquid water.The absorption liquid (rare nitric acid) that descends from top to bottom along denitrating tower gets at the bottom of the denitration Tata, and is delivered to nitric acid product storage tank through pipeline 6.The T2 cat head comes out and the flue gas after out of stock is from the denitration absorption tower, gets into CO
2Absorption tower T3.CO
2Absorption tower T3 adopts packed tower, and 1.1 meters of tower diameters are high 5.5 meters.Hot potassium carbonate solution gets into CO from pipeline 9 through blender M2 as absorption liquid
2Absorption tower T3, flow does.Fully the flue gas after the contact is discharged from chimney through piping 7 after from cat head, because the acid ingredient in the flue gas all is removed allow compliance with emission standards basically at this moment.Absorb CO
2The hot potassium carbonate absorption liquid from CO
2Absorption tower T3 gets into CO through heat exchanger II E2 heating back
2Regenerator T4 utilizes the part Steam Heating of phase-splitter V1, makes temperature remain on about 120 ℃ CO
2Be to get into bulking system from the pipeline of cat head 11 with the flow after the desorb, the pressurization can obtains CO
2The manufacturing other products is sold or be used as to product.After the hot potassium carbonate solution process pump III P3 process heat exchanger II E2 heat exchange at the bottom of the tower, M2 is back to CO through blender
2Absorption tower T3 recycles.
Claims (7)
1. technology of utilizing the flue gas waste heat to remove its sour gas, it is made up of desulphurization system, denitrating system and decarbonization system, it is characterized in that it may further comprise the steps:
(1) the flue gas first passes through the electric dust collector, the flue gas to remove most of the dust, and then through the flue gas duct (2) into the heat exchanger through Ⅰ (E1) in the water in the tube, smoke said gas on the shell side, through the heat exchanger, the lower the temperature of the flue gas, into the desulfurization absorption column (T1), and the tube is heated in the water vaporized into the phase separator (V1), the water after the phase separation Return to the heat exchanger Ⅰ (E1), the heat exchanger Ⅰ (E1) and a phase separator (V1) equivalent to a combination of a waste heat boiler, the steam pressure of 3-6 atmospheres, and the water vapor through the shunt (S1) is divided into three strands, respectively, into the low-pressure turbine Ⅰ (TU1) and the low pressure turbine Ⅱ (TU2) and a heater (H1), the low pressure turbine driving steam Ⅰ (TU1), the turbine (TU1) a refrigerator (C1) of the power source, the refrigerator (C1) cooling, thereby obtaining chilled water, chilled water through the shunt (S2) were sent to the cooler Ⅰ (C2), the cooler Ⅱ (C3) and a cooler Ⅲ (C4) as desulfurization absorption column (T1), denitrification absorber (T2) and CO
2 absorption column (T3) of the refrigerant, so that the desulfurization absorption column (T1), denitrification absorber (T2) and CO
2 absorption column (T3) temperatures were maintained at their desired temperature, for driving a second stream of low-pressure steam turbine Ⅱ (TU2), the turbine Ⅱ (TU2 ) as a compressor (CO1) of the power source, the compressor (CO1) acting, and compressed by the desulfurization absorption column (T1) of the flue gas exhaust top to a pressure increased by a slight positive pressure to 0.25MPa or more, and into the denitrification absorber (T2), to remove NOx,? while producing nitric acid, and the third share of steam by the heater (H1) for the CO
2 regeneration tower (T4) provided heat to regenerate the CO
2 absorption liquid, recycling;
(2) flue gas through heat exchanger I (E1) heat exchange gets into desulfuration absorbing tower (T1) bottom; Fully contact with sulphur absorption liquid (being generally the mixed solution of calcium hydroxide and NaOH) from desulfuration absorbing tower (T1) top duct (3) charging; Flue gas after the desulfurization is discharged from desulfuration absorbing tower (T1) top; After the air that gets into from pipeline 12 mixes; Entering is by in steam turbine II (TU2) compressor driven (CO1); Make the pressure of gas be increased to the above back of 0.25MPa from entering denitration absorption tower, bottom (T2); The sulphur absorption liquid then drops to tower bottom along desulfurizing tower; Remove solid phase through Separation of Solid and Liquid, liquid phase can return the doctor solution liquid pool and recycle;
(3) after flue gas and the AIR MIXTURES after the pressurization got into denitration absorption tower (T2), with the NOx absorption liquid counter current contacting that pipeline (5) through top, denitration absorption tower (T2) gets into, the discharge of (T2) cat head got into CO again from the denitration absorption tower
2Absorption tower (T3), and the absorption liquid (rare nitric acid) that descends from top to bottom along denitrating tower gets at the bottom of the denitration Tata, and be delivered to nitric acid product storage tank through pipeline (6);
(4) flue gas after the denitration gets into CO from the bottom
2Absorption tower (T3), CO
2Absorption liquid generally adopts hot potassium carbonate solution or organic amine, the CO in the flue gas
2After in decarbonizing tower (T3), being absorbed, discharge through pipeline (7) from cat head, at this moment the acid ingredient in the flue gas all is removed basically, and wherein, SOx and NOx can be controlled in 50ml/m respectively
3And 30ml/m
3Below, CO
2Then can be lower than 5000ml/m
3Below, from CO
2The CO that absorption tower (T3) descends from top to bottom
2Absorption liquid gets into CO after then delivering to heat exchanger II (E2) heat exchange through column bottoms pump
2Regenerator (T4) top;
(5) at CO
2CO in the regenerator (T4)
2Again separated sucking-off, get into bulking system from cat head through piping (11), the pressurization can obtains CO
2The manufacturing other products is sold or be used as to product, the CO after the regeneration
2Absorption liquid is through CO
2After returning heat exchanger II (E2) heat exchange through pump III (P3) at the bottom of regenerator (T4) tower, get into decarburization absorption tower (T3) through blender (M2) and recycle; CO
2The heat that regenerator (T4) needs is obtained by the steam heater via (H1) that phase-splitter (V1) provides; And returning blender (M1) through pump I (P1), the liquid that condensation is got off recycles; The refrigerant of cooler I (C2), cooler II (C3) and cooler III (C4) outlet then passes through pump II (P2) blowback and to refrigerant refrigeration machine C1, freezes once more, recycles.
2. the technology that removes its sour gas according to claim 1; It is characterized in that: the removal methods of described oxysulfide is selected the mixed solution of calcium hydroxide and NaOH; Calcium hydroxide and NaOH mass fraction are that 10-40%, calcium hydroxide and NaOH mass ratio are 4:1 in the solution; As absorption liquid; It is more than 120 ℃ that flue gas advances to absorb the Tata temperature, and the oxysulfide removal efficiency is more than 90%.
3. the technology that removes its sour gas according to claim 1; It is characterized in that: the removal methods of described nitrogen oxide selects to use empty G&W as absorption liquid; Temperature remains on 5 ~ 30 ℃, and contain the flue gas of NOx and the ratio of air and confirm that method is following: 1 volume NO consumes the O of 0.75 volume
2, 1 volume NO
2Consume the O of 0.25 volume
2, contain the O of 0.2 volume in 1 volumes of air
2According to NO, NO in the flue gas
2Content, ratio and flow, calculate the theoretical air flow, actual air flow is 1.5 ~ 2:1 with the ratio of theoretical air flow, thereby draws the amount of required actual air.
4. the technology that removes its sour gas according to claim 1 is characterized in that: described CO
2Removal methods generally adopt hot potassium carbonate solution or organic amine as absorption liquid; Absorption reaction is reversible reaction; Temperature need remain on required separately temperature, and organic amine remains on 20 ~ 40 ℃ as the absorption liquid temperature, and the hot potassium carbonate solution temperature need remain on 95 ~ 105 ℃.
5. the technology that removes its sour gas according to claim 4 is characterized in that: described organic amine is monoethanolamine, diethanol amine, triethanolamine or N monomethyl diethanol amine.
6. the technology that removes its sour gas according to claim 1 is characterized in that: described CO
2Renovation process select to use Steam Heating, make temperature remain on 110 ℃ and get final product.
7. the technology that removes its sour gas according to claim 1 is characterized in that: according to nitrogen-containing oxide whether in the flue gas, whether need the denitrification step of denitration absorption tower T2 in the decision technology.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011103061323A CN102343201A (en) | 2011-10-11 | 2011-10-11 | Process for removing acid gas from flue gas by using residual heat of flue gas |
| PCT/CN2012/076048 WO2013053235A1 (en) | 2011-10-11 | 2012-05-25 | Process for removing acid gas from flue gas by using waste heat of same |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011103061323A CN102343201A (en) | 2011-10-11 | 2011-10-11 | Process for removing acid gas from flue gas by using residual heat of flue gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102343201A true CN102343201A (en) | 2012-02-08 |
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| CN102600708A (en) * | 2012-03-07 | 2012-07-25 | 杭州恒明环境技术有限公司 | High-efficiency low-cost purification process of flue gas |
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| WO2013053235A1 (en) * | 2011-10-11 | 2013-04-18 | 南京大学 | Process for removing acid gas from flue gas by using waste heat of same |
| CN103432861A (en) * | 2013-09-24 | 2013-12-11 | 中国五冶集团有限公司 | Sintering desulfurization and white smoke removal system and technological process of sintering desulfurization and white smoke removal system |
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| CN102343201A (en) * | 2011-10-11 | 2012-02-08 | 南京大学 | Process for removing acid gas from flue gas by using residual heat of flue gas |
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