CN116603369A - Absorbent capable of efficiently absorbing sulfur dioxide - Google Patents
Absorbent capable of efficiently absorbing sulfur dioxide Download PDFInfo
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- CN116603369A CN116603369A CN202310476418.9A CN202310476418A CN116603369A CN 116603369 A CN116603369 A CN 116603369A CN 202310476418 A CN202310476418 A CN 202310476418A CN 116603369 A CN116603369 A CN 116603369A
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- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 title claims abstract description 152
- 230000002745 absorbent Effects 0.000 title claims abstract description 57
- 239000002250 absorbent Substances 0.000 title claims abstract description 57
- 239000007789 gas Substances 0.000 claims abstract description 161
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 129
- 238000010521 absorption reaction Methods 0.000 claims abstract description 117
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 69
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 69
- 239000011593 sulfur Substances 0.000 claims abstract description 69
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 60
- 239000003546 flue gas Substances 0.000 claims abstract description 60
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 claims abstract description 28
- IUXYVKZUDNLISR-UHFFFAOYSA-N 2-(tert-butylamino)ethanol Chemical compound CC(C)(C)NCCO IUXYVKZUDNLISR-UHFFFAOYSA-N 0.000 claims abstract description 19
- LHIJANUOQQMGNT-UHFFFAOYSA-N aminoethylethanolamine Chemical compound NCCNCCO LHIJANUOQQMGNT-UHFFFAOYSA-N 0.000 claims abstract description 19
- VARKIGWTYBUWNT-UHFFFAOYSA-N 2-[4-(2-hydroxyethyl)piperazin-1-yl]ethanol Chemical compound OCCN1CCN(CCO)CC1 VARKIGWTYBUWNT-UHFFFAOYSA-N 0.000 claims abstract description 18
- WFCSWCVEJLETKA-UHFFFAOYSA-N 2-piperazin-1-ylethanol Chemical compound OCCN1CCNCC1 WFCSWCVEJLETKA-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000007788 liquid Substances 0.000 claims description 198
- 238000005406 washing Methods 0.000 claims description 116
- 230000008929 regeneration Effects 0.000 claims description 113
- 238000011069 regeneration method Methods 0.000 claims description 113
- 238000011084 recovery Methods 0.000 claims description 68
- 238000010992 reflux Methods 0.000 claims description 32
- 238000006477 desulfuration reaction Methods 0.000 claims description 19
- 230000023556 desulfurization Effects 0.000 claims description 19
- 238000001914 filtration Methods 0.000 claims description 12
- 238000010438 heat treatment Methods 0.000 claims description 10
- 239000013505 freshwater Substances 0.000 claims description 9
- 238000009826 distribution Methods 0.000 claims description 7
- 239000002351 wastewater Substances 0.000 claims description 7
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- AHXXIYFEJGGBMG-UHFFFAOYSA-N 1-[2-(tert-butylamino)ethoxy]ethanol Chemical compound CC(O)OCCNC(C)(C)C AHXXIYFEJGGBMG-UHFFFAOYSA-N 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 229910021642 ultra pure water Inorganic materials 0.000 claims description 2
- 239000012498 ultrapure water Substances 0.000 claims description 2
- 239000003973 paint Substances 0.000 claims 1
- 239000002253 acid Substances 0.000 abstract description 8
- 238000003723 Smelting Methods 0.000 abstract description 4
- 239000006227 byproduct Substances 0.000 abstract description 4
- 238000000746 purification Methods 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000000047 product Substances 0.000 abstract description 2
- 230000009102 absorption Effects 0.000 description 82
- 239000000243 solution Substances 0.000 description 28
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 14
- 238000000034 method Methods 0.000 description 13
- 239000006096 absorbing agent Substances 0.000 description 12
- 230000002378 acidificating effect Effects 0.000 description 9
- 230000008569 process Effects 0.000 description 8
- 239000000428 dust Substances 0.000 description 7
- 238000001816 cooling Methods 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 6
- 230000006872 improvement Effects 0.000 description 5
- 239000012535 impurity Substances 0.000 description 5
- 239000003595 mist Substances 0.000 description 5
- 238000004064 recycling Methods 0.000 description 4
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 3
- 230000003749 cleanliness Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000000779 smoke Substances 0.000 description 3
- 239000001509 sodium citrate Substances 0.000 description 3
- NLJMYIDDQXHKNR-UHFFFAOYSA-K sodium citrate Chemical compound O.O.[Na+].[Na+].[Na+].[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O NLJMYIDDQXHKNR-UHFFFAOYSA-K 0.000 description 3
- 235000010265 sodium sulphite Nutrition 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000003916 acid precipitation Methods 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000002608 ionic liquid Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009103 reabsorption Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000007853 buffer solution Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 238000007405 data analysis Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000383 hazardous chemical Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 230000001953 sensory effect Effects 0.000 description 1
- 239000004289 sodium hydrogen sulphite Substances 0.000 description 1
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
- 239000002699 waste material Substances 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
- B01D53/14—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
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/50—Combinations of absorbents
- B01D2252/504—Mixtures of two or more absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (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 high-efficiency absorbing sulfur dioxide absorbent, which relates to the technical field of environmental protection flue gas treatment, and is used for removing sulfur dioxide from two or more mixed gases in smelting flue gas, ring-collected flue gas, claus tail gas, acid making tail gas and boiler tail gas, and recovering high-concentration sulfur dioxide, wherein the high-efficiency absorbent provided by the invention comprises, by mass, 25-40% of N, N' -bis (2-hydroxyethyl) piperazine, 1-6% of piperazine, 2-8% of N- (2-hydroxyethyl) ethylenediamine, 2-10% of N-hydroxyethyl piperazine, 0.02-0.1% of tert-butylaminoethanol and 40-49% of water. The efficient absorbent has the advantages of high sulfur dioxide absorption selectivity, high sulfur capacity, high sulfur dioxide purification degree in the absorbed flue gas, high-concentration sulfur dioxide as a byproduct, and the like for producing sulfur products with economic values.
Description
Technical Field
The invention relates to the technical field of environmental protection tail gas treatment, in particular to an efficient sulfur dioxide absorption agent.
Background
Acid rain is one of three global environmental hazards. SO discharged from air 2 Approximately 90% of SO is emitted from coal-fired flue gas due to combustion of coal 2 Is the main cause of acid rain hazard, however SO 2 The method is a necessary raw material for producing sulfuric acid, sulfur and the like while bringing harm.
In the 70 s of the 20 th century, the W-L method, namely, the method of absorbing SO2 by using a mixed solution of sodium sulfite and sodium bisulphite and recovering SO2 by heating and desorbing, is developed by Wellman-Lord corporation in the United states, but the sodium sulfite is easily oxidized into sodium sulfate by adopting the method, SO that the recycling of the absorption liquid is not facilitated.
1983. In the years, mekiney replaced sodium sulfite with a buffer solution of citric acid and sodium citrate, although sodium citrate is responsible for the absorbed SO 2 Has strong oxidation resistance, but sodium citrate has degradation phenomenon in the desorption process.
Disclosure of Invention
The invention aims to provide an absorbent capable of efficiently absorbing sulfur dioxide.
In order to achieve the above purpose, the invention is implemented according to the following technical scheme:
the efficient sulfur dioxide absorbing agent consists of 25-40% of N, N' -bis (2-hydroxyethyl) piperazine, 1-6% of piperazine, 2-8% of N- (2-hydroxyethyl) ethylenediamine, 2-10% of N- (2-hydroxyethyl) ethylenediamine, 0.02-0.1% of tert-butylaminoethanol and 40-49% of water according to mass concentration.
Preferably, the N, N' -bis (2-hydroxyethyl) piperazine accounts for 39% by mass, the N-hydroxyethyl piperazine accounts for 6%, the piperazine accounts for 3%, the N- (2-hydroxyethyl) ethylenediamine accounts for 3%, the tert-butylaminoethanol accounts for 0.06%, and the balance is water, wherein the water is desalted water or ultrapure water.
As another improvement, the N, N' -bis (2-hydroxyethyl) piperazine, N- (2-hydroxyethyl) ethylenediamine, N-hydroxyethyl piperazine, tert-butylaminoethanol and water are removed, tert-butylaminoethanol is used instead of tert-butylaminoethanol, and the water is used instead of desalted water, and the specific formula is: according to the mass concentration, the N, N' -bis (2-hydroxyethyl) piperazine is 38%, the piperazine is 5.8%, the N- (2-hydroxyethyl) ethylenediamine is 8%, the tert-butylaminoethoxy ethanol is 0.09%, and the rest components are desalted water.
As another improvement, the N, N' -bis (2-hydroxyethyl) piperazine accounts for 36%, the N-hydroxyethyl piperazine accounts for 7.5%, the piperazine accounts for 4.8%, the N- (2-hydroxyethyl) ethylenediamine accounts for 3%, the tert-butylaminoethanol accounts for 0.03%, the balance is water, and the water is desalted water.
As another improvement, the mass concentration of the N, N' -bis (2-hydroxyethyl) piperazine is 40%, the N-hydroxyethyl piperazine is 5.8%, the piperazine is 2.2%, the N- (2-hydroxyethyl) ethylenediamine is 2.2%, the tert-butylaminoethanol is 0.07%, and the rest is water, wherein the water is desalted water.
Preferably, the pH value of the high-efficiency sulfur dioxide absorption agent is 9-12.
The desulfurization system adopting the efficient sulfur dioxide absorbent comprises a washing tower, an electric demister, an absorption tower, a ring collection recovery tank, a regeneration tower, a regeneration gas separator, a sulfur tail absorption tower, a sulfur tail recovery tank, a washing pump, a ring collection liquid pump, a ring collection lean liquid pump, a ring collection recovery pump, a sulfur tail lean liquid pump, a sulfur tail rich liquid pump, a reflux pump, a sulfur tail recovery pump, a ring collection lean liquid cooler, a lean rich liquid heat exchanger, a reboiler, a sulfur tail lean liquid cooler, a filtering device and a regeneration gas cooler, wherein the gas inlet end of the washing tower is connected with the ring collection flue gas, the water inlet end of the washing tower is connected with fresh water for production, the gas outlet end of the upper end of the washing tower is connected with the gas inlet end of the electric demister, the water outlet end of the washing tower is simultaneously connected with the washing liquid distributor end of the washing tower, the water inlet end of the filtering device and a wastewater discharge pipe, the drainage end of the filtering device is connected with the lower part of the washing tower, the exhaust end of the electric demister is connected with the air inlet end of the absorption tower, the washing flue gas is recovered in the annular collection recovery tank to carry the high-efficiency absorption sulfur dioxide absorbent, the absorbent inlet of the absorption tower is connected with the outlet of the annular collection recovery tank through the annular collection recovery pump, the absorbent recovery end of the absorption tower is connected with the inlet of the annular collection recovery tank, the lean solution inlet of the absorption tower is connected with the outlet of the annular collection lean solution cooler, the rich solution inlet of the absorption tower is connected with the liquid outlet of the sulfur tail absorption tower through the sulfur tail rich solution pump, the liquid outlet of the absorption tower is connected with the first inlet of the lean and rich solution heat exchanger through the annular collection rich solution pump, the top of the absorption tower is provided with a purified gas outlet, the first outlet of the lean-rich liquid heat exchanger is respectively connected with the inlet of the lean-lean liquid loop pump and the inlet of the sulfur tail lean liquid loop pump, the outlet of the lean-lean liquid loop pump is connected with the inlet of the lean-lean liquid loop cooler, the second outlet of the lean-rich liquid heat exchanger is connected with the inlet of the regeneration tower, the second inlet of the lean-rich liquid heat exchanger is connected with the outlet of the regeneration tower, the outlet of the sulfur tail lean liquid pump is connected with the inlet of the sulfur tail absorption tower through the sulfur tail lean liquid loop cooler, the circulation interface of the regeneration tower is connected with the inlet and outlet of the reboiler, the reboiler is connected with low-pressure steam, the exhaust end of the regeneration tower is connected with the inlet end of the regeneration gas separator through the reflux pump, the exhaust end of the regeneration gas separator discharges sulfur dioxide gas, the sulfur tail absorption liquid distributor end is connected with the outlet of the sulfur tail absorption tower through the sulfur tail pump, and the exhaust end of the sulfur tail gas recovery tower reaches the exhaust end of the sulfur recovery tower is connected with the exhaust outlet of the sulfur recovery tower.
As an improvement, the desulfurization system adopting the high-efficiency absorption sulfur dioxide absorbent comprises a washing tower, a washing pump, a ring collection absorption tower, a rich liquid pump, a lean liquid heat exchanger, a lean liquid pump, a lean liquid heat exchanger, a regeneration tower, a reboiler, a regeneration gas separator, a reflux pump, a regenerated gas cooler, an electric demister and an absorption electric demister, wherein the air inlet end of the washing tower is connected with flue gas, the water inlet end of the washing tower is connected with new water, the water outlet end of the washing tower is connected with the water inlet end of the washing pump, the water outlet end of the washing pump is simultaneously connected with a wastewater discharge pipe and the water inlet end of a washing liquid distributor of the washing tower, the air outlet end of the washing tower is connected with the air inlet end of the electric demister, the air outlet end of the electric demister is connected with the air inlet end of the electric demister, the lower section of the ring collection absorption tower stores the high-efficiency absorbent, the liquid outlet end of the ring collection absorption tower is connected with the first inlet of the rich liquid heat exchanger through the rich liquid pump, the water outlet end of the ring collection absorption tower is connected with the first inlet end of the lean liquid heat exchanger, the water outlet end of the electric demister is connected with the second inlet end of the electric demister, the upper end of the electric demister is connected with the air inlet end of the electric demister is connected with the second inlet end of the electric demister through the air inlet end of the electric demister, the upper end of the electric demister is connected with the second inlet end of the electric demister, and the electric demister is connected with the second inlet end of the electric demister, the liquid discharge end of the regeneration gas separator is connected with the reflux liquid distributor end of the regeneration tower through the reflux pump, the exhaust end of the regeneration gas separator discharges sulfur dioxide gas, the reboiling circulation heating end of the regeneration tower is connected with the inlet and outlet ends of the reboiler, and the reboiler is connected with low-pressure steam.
As an improvement, a desulfurization system adopting the high-efficiency absorption sulfur dioxide absorbent comprises a washing tower, a washing pump, an absorption tower, a rich liquid pump, a lean liquid heat exchanger, a lean liquid pump, a lean liquid heat exchanger, a regeneration tower, a reboiler, a regeneration gas separator, a reflux pump, a regenerated gas cooler, an electric demister, a recovery tank, a recovery pump and an exhaust fan, wherein the air inlet end of the washing tower is connected with flue gas, the water inlet end of the washing tower is connected with new water for production, the water outlet end of the washing tower is connected with the water inlet end of the washing pump, the water outlet end of the washing pump is simultaneously connected with the water inlet end of the washing tower and a waste water discharge pipe, the air outlet end of the washing tower is connected with the air inlet end of the electric demister, the air outlet end of the electric demister is connected with the air inlet end of the absorption tower, the lower section in the absorption tower stores the high-efficiency absorption sulfur dioxide absorbent, the liquid discharge end of the absorption tower is connected with the first inlet of the rich liquid heat exchanger through the rich liquid pump, the liquid outlet end of the absorption tower is connected with the first inlet of the lean liquid heat exchanger, the liquid discharge end of the absorption tower is connected with the air outlet end of the absorption tower is connected with the second inlet end of the absorption tower through the exhaust gas separator, the liquid discharge end of the absorption tower is connected with the air inlet of the regeneration tower is connected with the air inlet end of the regeneration tower, the exhaust gas is connected with the air outlet of the recovery end of the recovery tower through the lean liquid of the exhaust gas separator, the exhaust gas is connected with the second inlet end of the recovery end of the electric demister, the liquid discharge end of the regeneration gas separator is connected with the reflux liquid distribution end of the regeneration tower through the reflux pump, the exhaust end of the regeneration gas separator discharges sulfur dioxide gas, the reboiling heating circulation end of the regeneration tower is connected with the inlet and outlet of the reboiler, and the heating end of the reboiler is connected with low-pressure steam.
The beneficial effects of the invention are as follows:
compared with the prior art, the invention has the following technical effects:
1. generally has no vapor pressure, and does not generate harmful gas which pollutes the atmosphere in the using process;
2. the physical and chemical properties of the absorbent can be regulated by adopting the sulfate radical content generated in the control system, namely the absorbent has excellent designability, and the ionic liquid with special functions can be obtained through molecular design.
3. Can be recycled and has low loss.
4. By-product of 99% dry SO at the same time of desulfurizing ２ The byproducts can be used as excellent raw materials of liquid sulfur dioxide, sulfuric acid, sulfur or other vulcanized products.
5. The desulfurization efficiency is high, the highest desulfurization efficiency can reach 99.9%, and the desulfurization efficiency can be flexibly adjusted.
6. The application range is wide, the operation is stable in the range of 0.02 to 5 percent of the sulfur content in the flue gas, and the method can adapt to the large-scale change of the sulfur content in the flue gas.
Drawings
FIG. 1 is a graph of the absorption equilibrium of the high-efficiency sulfur dioxide absorbent of the present invention at 52 ℃;
FIG. 2 is a schematic diagram of a desulfurization system for efficiently absorbing sulfur dioxide absorbent according to embodiment 1 of the present invention;
FIG. 3 is a schematic diagram of a desulfurization system for efficiently absorbing sulfur dioxide absorbent according to example 2 of the present invention;
FIG. 4 is a schematic diagram of the structure of a desulfurization system for efficiently absorbing sulfur dioxide absorbent according to example 3 of the present invention.
In fig. 2: a washing tower 1, an electric demister 2, an absorption tower 3, a ring collection recovery tank 4, a regeneration tower 5, a regeneration gas separator 6, a sulfur tail absorption tower 7, a sulfur tail recovery tank 8, a washing pump 9, a ring collection rich liquid pump 10, a ring collection lean liquid pump 11, a ring collection recovery pump 12, a sulfur tail lean liquid pump 13, a sulfur tail rich liquid pump 14, a reflux pump 15, a sulfur tail recovery pump 16, a ring collection lean liquid cooler 17, a lean-rich liquid heat exchanger 18, a reboiler 19, a sulfur tail lean liquid cooler 20, a filtering device 21, a regenerated gas cooler 22 and the washing tower 1;
in fig. 3: a washing pump 9, a ring-collecting absorption tower 203, a rich liquid pump 204, a lean liquid heat exchanger 205, a lean liquid pump 206, a lean rich liquid heat exchanger 18, a regeneration tower 5, a reboiler 19, a regeneration gas separator 6, a reflux pump 15, a regeneration gas cooler 22, an electric demister 2 and an absorption electric demister 2014;
in fig. 4: a washing tower 1, a washing pump 9, an absorption tower 3, a rich liquid pump 204, a lean liquid heat exchanger 205, a lean liquid pump 206, a lean rich liquid heat exchanger 18, a regeneration tower 5, a reboiler 19, a regeneration gas separator 6, a reflux pump 15, a regeneration gas cooler 22, an electric demister 2, a recovery tank 3014, a recovery pump 3015 and an exhaust fan 3016.
Detailed Description
The invention will be further described with reference to the accompanying drawings and specific embodiments, wherein the exemplary embodiments and descriptions of the invention are for purposes of illustration, but are not intended to be limiting.
The sulfur dioxide absorbent for the high-efficiency absorption of the sulfur dioxide is composed of 25-40% of N, N' -bis (2-hydroxyethyl) piperazine, 1-6% of piperazine, 2-8% of N- (2-hydroxyethyl) ethylenediamine, 2-10% of N- (2-hydroxyethyl) piperazine, 0.02-0.1% of tert-butylaminoethanol and 40-49% of water according to mass concentration.
Preferably, the pH value of the high-efficiency sulfur dioxide absorption agent is 9-12.
As shown in fig. 1: placing the absorption bottle in a water bath constant temperature box, connecting a pipeline between an experiment air source and the absorption bottle, and arranging a flowmeter and SO (SO) in the air 2 A concentration detection port, and a pipeline and SO are arranged behind the absorption bottle 2 A concentration detection port. Adding an absorbent into an absorption bottle, and dropwise adding the absorbent into the absorption bottle according to the mass ratio of 1:2, adjusting the water bath constant temperature box to 52 ℃, and after the temperature is constant, introducing SO-containing air to prepare 2 The gas source of the gas, the flow rate is regulated, the ventilation time is 3h, and the volume of the absorbent is kept unchanged by supplementing desalted water in the experimental process. Determination of liquid phase SO in absorbent after the end of experiment 2 Is contained in the composition.
The absorbent comprises the following components: 17% of N, N' -bis (2-hydroxyethyl) piperazine, 2.6% of piperazine, 3.6% of N- (2-hydroxyethyl) ethylenediamine, 0.04% of tert-butylaminoethoxyethanol, and the balance of desalted water.
The following measurements were made at different SOs 2 At a concentration, the absorbent absorbs liquid phase SO at 52 DEG C 2 Is contained in the composition.
Embodiment 1 a desulfurization system for efficiently absorbing sulfur dioxide absorbent comprises a washing tower 1, an electric demister 2, an absorption tower 3, an annular collection recovery tank 4, a regeneration tower 5, a regeneration gas separator 6, a sulfur tail absorption tower 7, a sulfur tail recovery tank 8, a washing pump 9, an annular collection rich liquid pump 10, an annular collection lean liquid pump 11, an annular collection recovery pump 12, a sulfur tail lean liquid pump 13, a sulfur tail rich liquid pump 14, a reflux pump 15, a sulfur tail recovery pump 16, an annular collection lean liquid cooler 17, a lean liquid heat exchanger 18, a reboiler 19, a sulfur tail lean liquid cooler 20, a filtering device 21, a regeneration gas cooler 22, an air inlet end of the washing tower 1 is connected with annular collection flue gas, an air inlet end of the washing tower 1 is connected with fresh water, an air outlet end of the upper end of the washing tower 1 is connected with an air inlet end of the electric demister 2, a water outlet end of the washing tower 1 is connected with an air inlet end of the washing pump 9, a water outlet end of the washing pump 9 is simultaneously connected with a washing liquid distribution end of the washing tower 1, a filtering device 21, an air inlet end of the filtering device is connected with an air inlet end of the exhaust pipe 3 of the annular collection recovery tank 4, an air outlet of the filtering device is connected with the exhaust gas collector 3 of the exhaust gas absorber 4, an air inlet of the exhaust end of the absorption tower 1 is connected with the exhaust gas absorber 4 is connected with the exhaust gas collector 4, an inlet of the exhaust gas collector 4 is connected with the exhaust gas collector 2, an inlet of the exhaust gas collector is connected with the exhaust gas collector 3 of the exhaust gas collector is connected with the exhaust gas collector 2, the liquid discharge port of the absorption tower 3 is connected with the first inlet of the lean-rich liquid heat exchanger 18 through the annular collecting rich liquid pump 10, the top of the absorption tower 3 is provided with an exhaust gas discharge port, the first outlet of the lean-rich liquid heat exchanger 18 is respectively connected with the inlet of the annular collecting lean liquid pump 11 and the inlet of the sulfur tail lean liquid pump 13, the outlet of the annular collecting lean liquid pump 11 is connected with the inlet of the annular collecting lean liquid cooler 17, the second outlet of the lean-rich liquid heat exchanger 18 is connected with the inlet of the regeneration tower 5, the second inlet of the lean-rich liquid heat exchanger 18 is connected with the outlet of the regeneration tower 5, the outlet of the sulfur tail lean liquid pump 13 is connected with the inlet of the sulfur tail absorption tower 7 through the sulfur tail liquid cooler 20, the circulation interface of the regeneration tower 5 is connected with the inlet of the reboiler 19, the exhaust end of the regeneration tower 5 is connected with the inlet of the regeneration tower 6 through the regeneration gas cooler 22, the exhaust gas reflux end of the regeneration tower 6 is connected with the exhaust gas inlet of the exhaust gas recovery tower 7 through the exhaust gas reflux end of the exhaust gas recovery tower 8, and the exhaust gas of the recovery tower 7 is connected with the exhaust gas of the exhaust gas recovery tower 7 through the exhaust gas recovery tower 6.
The environment smoke collection of a smelting workshop and the sulfuric acid tail gas of a sulfuric acid workshop are mainly treated in a copper factory, two paths of smoke are respectively absorbed, and a set of regeneration system process is shared, so that the occupied area and the investment are saved.
The gas volume in the ring-collected flue gas is 660000Nm 3 And/h, the pressure is 4.5Kpa, the temperature is 57-80 ℃, and the average SO in the flue gas is equal 2 At a concentration of 2027mg/Nm, where SO 2 The peak concentration was 10000 mg/Nm, the trough was 800 mg/Nm. Dust concentration is 95mg/Nm, dust component: cu (25.14%), as (7.96%), pb (4.67%) and the tail gas SO are required 2 The discharge is less than or equal to 65mg/Nm 3 。
Exhaust gas flow of sulfuric acid tail gas 165000Nm 3 And/h, the pressure is 3Kpa, the temperature is 70 ℃, and the acid mist content is as follows: 30 mg/Nm 3 ，
Average SO in flue gas 2 Concentration of 0.01%, and requires tail gas SO 2 The discharge is less than or equal to 65mg/Nm 3 。
As shown in the process flow chart of figure 2, the ring-collected flue gas firstly enters a washing tower (1), the washing tower (1) is used for humidifying and cooling the ring-collected flue gas to below 40 ℃, impurities such as dust and the like in the ring-collected flue gas are removed, washing water is pressurized by a washing pump (9), most of the washing water is sent to the upper part of the water washing tower, the washing flue gas is circulated, a small part of the washing water enters a filtering device (21) for dedusting and impurity removal, and filtered clear liquid returns to the washing tower (1). Part of the washing water is periodically discharged and the fresh water is replenished to maintain the cleanliness of the washing water. An electric demister (2) is arranged at the top of the washing tower (1) to further remove dust and acid mist carried by the washed ring-collected flue gas, and solid and liquid impurities and acid mist of the ring-collected flue gas are reduced better.
The purified ring-collected flue gas enters the bottom of an absorption tower (3) and is in countercurrent contact with an absorbent from top to bottom in the tower body, sulfur dioxide in the ring-collected flue gas is absorbed and trapped in the absorbent, the ring-collected flue gas enters a recovery section of the absorption tower (3) after being purified by removing sulfur dioxide, the ring-collected flue gas is washed and recovered by a ring-collected recovery pump (12) after being provided with circulating power for circulating washing, the trace absorbent entrained in the flue gas is recovered, the recovered liquid of the trace absorbent is collected to a ring-collected recovery tank (4), and the flue gas is finally discharged to a chimney.
The absorbent absorbing sulfur dioxide is changed from lean solution into rich solution, and is pressurized by an annular rich solution collecting pump (10) at the bottom of an absorption tower (3) and sent to a lean rich solution heat exchanger (18), and enters a regeneration tower (5) after being subjected to heat exchange by high-temperature lean solution at 116-118 ℃; and the lean solution regenerated by the regeneration tower (5) is sent to the annular collection lean solution cooler (17) for further cooling to 42-45 ℃ by pressurizing a part of the lean solution after heat is recovered by the lean-rich solution heat exchanger (18) by the annular collection lean solution pump (11), and then sent to the upper part of the absorption tower (3) for re-absorbing sulfur dioxide. The other part is pressurized by a sulfur tail lean solution pump (13) and sent to a sulfur tail lean solution cooler (20) for further cooling to 45 ℃, then sent to the upper part of a sulfur tail absorption tower (7) for re-absorbing sulfur dioxide, and the rich solution absorbing the sulfur tail flue gas is returned to the absorption tower (3) after being pressurized by a sulfur tail rich solution pump (14). The upper part of the sulfur tail absorption tower (7) is also provided with a recovery section, and the flue gas is circularly washed by a sulfur tail recovery pump (16) to recover trace absorbent carried in the flue gas, the recovery liquid is collected to a sulfur tail recovery tank (8), and the purified sulfur tail flue gas is discharged to a chimney.
The rich liquid heated by the lean-rich liquid heat exchanger (18) and having the temperature of 95-98 ℃ is sent to the upper part of the regeneration tower (5), the absorbent is regenerated after being heated, the regenerated heat provided by the reboiler (19) at the bottom of the tower is evaporated to the top of the regeneration tower (5), the regenerated sulfur dioxide gas and the water vapor are cooled to 45 ℃ by the regenerated gas cooler (22), the water vapor is condensed into acidic water, the acidic water enters the regeneration gas separator (6), the liquid acidic water is sent back to the regeneration tower (5) by the reflux pump (15), and the sulfur dioxide gas is separated by the regeneration gas separator (6) and then sent to the post processes such as acid making and the like for recycling.
The composition of the absorbent diluted with desalted water is as follows:
12 percent of N, N' -bis (2-hydroxyethyl) piperazine (mass fraction), 2.5 percent of N-hydroxyethyl piperazine (mass fraction), 1.6 percent of piperazine, 1 percent of N- (2-hydroxyethyl) ethylenediamine (mass fraction), 0.01 percent of tert-butylaminoethanol (mass fraction) and the balance of desalted water.
The partial operation data are as follows:
from the analysis of operation data, the fluctuation of the flue gas amount and the concentration of sulfur dioxide in the flue gas has little influence on the concentration of sulfur dioxide in the tail gas emission, and the operation does not need to be adjusted.
Embodiment 2 a desulfurization system for efficiently absorbing sulfur dioxide absorbent comprises a scrubber 1, a scrubber 9, a ring-collecting absorber 203, a rich liquid pump 204, a lean liquid heat exchanger 205, a lean liquid pump 206, a lean liquid heat exchanger 18, a regenerator 5, a reboiler 19, a regeneration gas separator 6, a reflux pump 15, a regeneration gas cooler 22, an electric demister 2, and an absorption electric demister 2014, wherein the gas inlet of the scrubber 1 is connected with flue gas, the water inlet of the scrubber 1 is connected with fresh water, the water outlet of the scrubber 1 is connected with the water inlet of the scrubber 9, the water outlet of the scrubber 9 is simultaneously connected with a waste water discharge pipe and the water inlet of the scrubber 1, the gas outlet of the scrubber 1 is connected with the gas inlet of the electric demister 2, the gas outlet of the electric demister 2 is connected with the gas inlet of the ring-collecting absorber 203, the lower section of the ring-collecting absorber 203 stores the high-efficiency absorbent, the water inlet 205 is connected with the lean liquid inlet of the second separator 2014 through the lean liquid outlet of the expander 203, the lean liquid heat exchanger 205 is connected with the gas outlet of the regenerator 18, the lean liquid is connected with the gas outlet of the regenerator 18 at the gas outlet of the exhaust gas separator 2, the exhaust end of the exhaust gas separator 2 is connected with the exhaust gas outlet of the exhaust gas separator 2, the lean liquid 205 is connected with the gas inlet of the exhaust 2 through the exhaust gas separator 18, the exhaust gas outlet of the exhaust 2 is connected with the exhaust 2 of the exhaust gas separator is connected with the exhaust 2, the exhaust end of the regeneration tower 5 is connected with the inlet of the regeneration gas separator 6 through the regeneration gas cooler 22, the liquid discharge end of the regeneration gas separator 6 is connected with the reflux liquid distribution end of the regeneration tower 5 through the reflux pump 15, the exhaust end of the regeneration gas separator 6 discharges sulfur dioxide gas, the reboiling circulation heating end of the regeneration tower 5 is connected with the inlet and outlet ends of the reboiler 19, and the reboiler 19 is connected with low-pressure steam.
The flue gas desulfurization unit of a petroleum refining sulfur recovery device is mainly used for treating the tail gas of the outlet of a sulfur tail gas incinerator and byproducts (high-concentration SO) 2 Gas) is sent to a claus device to recycle SO 2 Is a target of (a).
51249Nm of Claus tail gas treatment 3 And/h, temperature: 170 ℃, pressure: 20KPa (g), SO2 content in the tail gas: 0.28%, require tail gas SO 2 The discharge is less than or equal to 100mg/Nm 3 。
As shown in the process flow chart of figure 3, firstly, flue gas enters a washing tower (1), contacts with washing water from top to bottom in a countercurrent manner in the tower body, and removes particles such as dust while quenching, washing and cooling, the washing water is circularly sprayed by providing power through a washing pump (9), the washing tower maintains the supplement of fresh water and the discharge of concentrated water so as to maintain the cleanliness of the washing water, an electric demister (2) is arranged at the top of the washing tower, so that mist washing water carried in the flue gas can be removed to further reduce solid and liquid impurities in the flue gas.
The flue gas after being washed and purified enters the bottom of the ring collection absorption tower (203) to be in countercurrent contact with the absorbent from top to bottom in the tower body, so that the sulfur dioxide in the flue gas is absorbed and trapped in the absorption liquid, and the flue gas enters the absorption electric demister (2014) after being desulfurized and purified, so that vaporific liquid drops carried by the flue gas are trapped, and the flue gas is washed back to the ring collection absorption tower (203), so that the loss of the absorbent is reduced. An absorption electric demister (2014) is arranged to reduce emission of acid mist and dust and improve the smoke emission sensory effect; the absorption liquid absorbing and capturing sulfur dioxide is changed into rich liquid from lean liquid, and is pressurized by a rich liquid pump (204) at the bottom of the absorption tower and sent to a lean-rich liquid heat exchanger (18), and the rich liquid is heated by the high-temperature lean liquid and then enters a regeneration system; and the lean solution regenerated by the regeneration system is sent to the lean solution heat exchanger (205) for further cooling by the lean solution pump (206) after heat is recovered by the lean solution heat exchanger (18), and then sent to the upper part of the annular collection absorption tower (203) for reabsorption of sulfur dioxide.
The rich liquid heated by the lean-rich liquid heat exchanger (18) is sent to the upper part of the regeneration tower (5), sulfur dioxide is regenerated after being heated, a reboiler (19) at the bottom of the tower provides regeneration heat of the absorption liquid, regenerated sulfur dioxide gas and water vapor are evaporated to the top of the tower and cooled by a regenerated gas cooler (22), the water vapor is condensed into acidic water, the acidic water enters a regeneration gas separator (6), the liquid acidic water is sent back to the regeneration tower (5) through a reflux pump (15), and the sulfur dioxide gas is sent to a Claus device for recycling after being separated by the regeneration gas separator (6).
The composition of the absorbent diluted with desalted water is as follows:
13 percent of N, N' -bis (2-hydroxyethyl) piperazine (mass fraction), 1 percent of piperazine (mass fraction), 2 percent of N-hydroxyethyl piperazine, 1 percent of N- (2-hydroxyethyl) ethylenediamine (mass fraction), 0.02 percent of tert-butylaminoethanol (mass fraction), and the balance of desalted water.
The partial operation data are as follows:
from the analysis of the operational data, a relatively stable gas source, SO, is directed at the concentration of sulfur dioxide in the flue gas 2 The removal efficiency is up to 99.5 percent.
Embodiment 3 a desulfurization system for efficiently absorbing sulfur dioxide absorbent comprises a washing tower 1, a washing pump 9, an absorption tower 3, a rich liquor pump 204, a lean liquor heat exchanger 205, a lean liquor pump 206, a lean rich liquor heat exchanger 18, a regeneration tower 5, a reboiler 19, a regeneration gas separator 6, a reflux pump 15, a regenerated gas cooler 22, an electric demister 2, a recovery tank 3014, a recovery pump 3015 and an exhaust fan 3016, wherein the gas inlet end of the washing tower 1 is connected with flue gas, the water inlet end of the washing tower 1 is connected with fresh water, the water outlet end of the washing tower 1 is connected with the water inlet end of the washing pump 9, the water outlet end of the washing pump 9 is simultaneously connected with the washing liquor distributor end and a waste water discharge pipe of the washing tower 1, the upper exhaust port of the washing tower 1 is connected with the gas inlet end of the electric demister 2, the gas outlet end of the electric demister 2 is connected with the gas inlet end of the absorption tower 3, the lower section in the absorber 3 stores the high-efficiency absorbing sulfur dioxide absorbent, the liquid discharge end of the absorber 3 is connected with the first inlet of the lean-rich liquid heat exchanger 18 through the rich liquid pump 204, the liquid distribution end of the absorber 3 is connected with the outlet of the recovery pump 3015, the liquid discharge end of the absorber 3 is connected with the water inlet end of the recovery pump 3015 through the recovery tank 3014, the exhaust end of the absorber 3 discharges tail gas through the exhaust fan 3016, the liquid distribution end of the absorber 3 is connected with the outlet of the lean liquid heat exchanger 205, the first outlet of the lean-rich liquid heat exchanger 18 is connected with the inlet of the lean-rich liquid heat exchanger 205 through the lean liquid pump 206, the second outlet of the lean-rich liquid heat exchanger 18 is connected with the air inlet end of the regenerator 5, the liquid discharge end of the regeneration tower 5 is connected with the second inlet of the lean-rich liquid heat exchanger 18, the air discharge end of the regeneration tower 5 is connected with the air inlet end of the regeneration gas separator 6 through the regeneration gas cooler 22, the liquid discharge end of the regeneration gas separator 6 is connected with the reflux liquid distributor end of the regeneration tower 5 through the reflux pump 15, the air discharge end of the regeneration gas separator 6 discharges sulfur dioxide gas, the reboiling heating circulation end of the regeneration tower 5 is connected with the inlet and outlet of the reboiler 19, and the heating end of the reboiler 19 is connected with low-pressure steam.
Clean regeneration item for waste lead acid storage battery in certain smeltingThe purpose is mainly to treat the flue gas of the oxygen-enriched side-blown smelting furnace, enter an ionic liquid desulfurization system, and absorb, analyze and enrich high-purity SO 2 Delivering to the front end of the precise purification and merging with part of the flue gas of the smelting furnace to enter a refined sulfuric acid system for producing refined sulfuric acid.
28500Nm of treated flue gas volume 3 And/h, temperature: 100+ -20deg.C, pressure: -2KPa (g), SO2 content in the tail gas: 1.75% of required tail gas SO 2 The discharge is less than or equal to 50mg/Nm 3 。
As shown in the process flow chart of figure 4, firstly, a washing tower (1) is in countercurrent contact with washing water from top to bottom in the tower body, particles such as dust are removed while the temperature is reduced, the washing water is circularly washed by supplying power through a washing pump (9), the washing tower (1) is used for keeping fresh water supplement and water discharge after concentration so as to keep the cleanliness of the washing water, an electric demister (2) is arranged at the top of the washing tower, and the mist-like washing water carried in flue gas can be removed to further reduce solid and liquid impurities in the flue gas;
the flue gas after washing and purifying enters the bottom of an absorption tower (3), contacts with absorption liquid from top to bottom in a tower body in a countercurrent way, absorbs and captures sulfur dioxide in the flue gas into the absorption liquid, after desulfurization and purification, enters a recovery section of the absorption tower, is circularly washed by the recovery liquid, washes and recovers trace absorption liquid carried in the flue gas, is finally pressurized by an exhaust fan (3016) and discharged to a chimney, recovers the recovery liquid of the trace absorption liquid, collects the recovery tank (3014), and provides circulating power for circularly washing flue tail gas by a recovery pump (3015); the absorption liquid absorbing and capturing sulfur dioxide is changed into rich liquid from lean liquid, and is pressurized by a rich liquid pump (204) at the bottom of the absorption tower and sent to a lean-rich liquid heat exchanger (18), and the rich liquid is heated by the high-temperature lean liquid and then enters a regeneration system; and the lean solution regenerated by the regeneration system is sent to the lean solution heat exchanger (205) for further cooling by the lean solution pump (206) after heat is recovered by the lean solution heat exchanger (18), and then sent to the upper part of the absorption tower for reabsorption of sulfur dioxide.
The rich liquid heated by the lean-rich liquid heat exchanger (18) is sent to the upper part of the regeneration tower (5), the rich liquid is heated and then regenerated by sulfur dioxide, a reboiler (19) at the bottom of the tower provides the regeneration heat of the absorption liquid, the regenerated sulfur dioxide gas and water vapor are evaporated to the top of the tower and cooled by a regenerated gas cooler (22), the water vapor is condensed into acidic water, the acidic water enters a regeneration gas separator (6), the liquid acidic water is sent back to the regeneration tower (5) through a reflux pump (15), and the sulfur dioxide gas is separated by the regeneration gas separator (6) and then sent to the post processes such as acid making and the like for recycling.
The composition of the absorbent diluted with desalted water is as follows:
the composition of the absorbent diluted with desalted water is as follows: 18 percent (mass fraction) of N, N' -bis (2-hydroxyethyl) piperazine, 1 percent (mass fraction) of N- (2-hydroxyethyl) ethylenediamine, 2.6 percent (mass fraction) of N-hydroxyethyl piperazine, 0.03 percent (mass fraction) of tert-butylaminoethanol, and the balance of desalted water.
The partial operation data are as follows:
| flue gas volume (Nm) 3 /h） | SO in flue gas 2 Content (%) | Tail row SO 2 Content (mg/Nm) 3 ） | SO 2 Removal efficiency (%) |
| 26635 | 1.80 | 38.90 | 99.93 |
| 28545 | 1.76 | 30.60 | 99.94 |
| 27380 | 1.78 | 29.80 | 99.94 |
From the operation data analysis, the tail gas can realize ultralow emission aiming at the gas source with higher and more stable sulfur dioxide concentration in the flue gas, and the desulfurization efficiency is higher.
The technical scheme of the invention is not limited to the specific embodiment, and all technical modifications made according to the technical scheme of the invention fall within the protection scope of the invention.
Claims (9)
1. An absorbent for efficiently absorbing sulfur dioxide, which is characterized in that: the water-based paint comprises, by mass, 25-40% of N, N' -bis (2-hydroxyethyl) piperazine, 1-6% of piperazine, 2-8% of N- (2-hydroxyethyl) ethylenediamine, 2-10% of N-hydroxyethyl piperazine, 0.02-0.1% of tert-butylaminoethanol and 40-49% of water.
2. The high-efficiency sulfur dioxide absorbent according to claim 1, wherein: according to the mass concentration, 39% of N, N' -bis (2-hydroxyethyl) piperazine, 6% of N-hydroxyethyl piperazine, 3% of N- (2-hydroxyethyl) ethylenediamine, 0.06% of tert-butylaminoethanol and the balance of water, wherein the water is desalted water or ultrapure water.
3. The high-efficiency sulfur dioxide absorbent according to claim 1, wherein: the N, N' -bis (2-hydroxyethyl) piperazine, N- (2-hydroxyethyl) ethylenediamine, N-hydroxyethyl piperazine, tert-butylaminoethanol and water are removed, tert-butylaminoethanol is adopted to replace the tert-butylaminoethanol, and desalted water is adopted to replace the water, wherein the specific formula is as follows: according to the mass concentration, the N, N' -bis (2-hydroxyethyl) piperazine is 38%, the piperazine is 5.8%, the N- (2-hydroxyethyl) ethylenediamine is 8%, the tert-butylaminoethoxy ethanol is 0.09%, and the rest components are desalted water.
4. The high-efficiency sulfur dioxide absorbent according to claim 1, wherein: according to mass concentration, the N, N' -bis (2-hydroxyethyl) piperazine accounts for 36%, the N-hydroxyethyl piperazine accounts for 7.5%, the piperazine accounts for 4.8%, the N- (2-hydroxyethyl) ethylenediamine accounts for 3%, the tert-butylaminoethanol accounts for 0.03%, the rest components are water, and the water is desalted water.
5. The high-efficiency sulfur dioxide absorbent according to claim 1, wherein: according to mass concentration, the N, N' -bis (2-hydroxyethyl) piperazine accounts for 40%, the N-hydroxyethyl piperazine accounts for 5.8%, the piperazine accounts for 2.2%, the N- (2-hydroxyethyl) ethylenediamine accounts for 2.2%, the tert-butylaminoethanol accounts for 0.07%, the rest components are water, and the water is desalted water.
6. The high-efficiency sulfur dioxide absorbent according to claim 1, wherein: the pH value of the high-efficiency sulfur dioxide absorption agent is 9-12.
7. A desulfurization system employing the high-efficiency sulfur dioxide absorbent according to claim 1, characterized in that: comprises a washing tower (1), an electric demister (2), an absorption tower (3), a ring collection recovery tank (4), a regeneration tower (5), a regeneration gas separator (6), a sulfur tail absorption tower (7), a sulfur tail recovery tank (8), a washing pump (9), a ring collection enrichment pump (10), a ring collection lean solution pump (11), a ring collection recovery pump (12), a sulfur tail lean solution pump (13), a sulfur tail rich solution pump (14), a reflux pump (15), a sulfur tail recovery pump (16), a ring collection lean solution cooler (17), a lean solution heat exchanger (18), a reboiler (19), a sulfur tail lean solution cooler (20), a filtering device (21) and a regeneration gas cooler (22), wherein the inlet end of the washing tower (1) is connected with ring collection flue gas, the inlet end of the washing tower (1) is connected with fresh water, the upper exhaust end of the washing tower (1) is connected with the inlet end of the electric demister (2), the water discharge end of the washing tower (1) is connected with the inlet end of the washing pump (9), the water discharge end of the washing tower (1) is connected with the water discharge end of the filtering device (21) and the water discharge end of the filtering device (21) are connected with the water discharge end of the washing tower (1), the exhaust end of the electric demister (2) is connected with the air inlet end of the absorption tower (3), the high-efficiency absorption sulfur dioxide absorbent is carried by the recovered washing flue gas in the ring concentration recovery tank (4), the absorbent inlet of the absorption tower (3) is connected with the outlet of the ring concentration recovery tank (4) through the ring concentration recovery pump (12), the absorbent recovery end of the absorption tower (3) is connected with the inlet of the ring concentration recovery tank (4), the lean liquid inlet of the absorption tower (3) is connected with the outlet of the ring concentration lean liquid cooler (17), the rich liquid inlet of the absorption tower (3) is connected with the liquid outlet of the sulfur tail absorption tower (7) through the sulfur tail rich liquid pump (14), the liquid outlet of the absorption tower (3) is connected with the first inlet of the lean liquid heat exchanger (18) through the ring concentration rich liquid pump (10), the top of the absorption tower (3) is provided with a purified gas discharge outlet, the lean liquid inlet of the rich liquid heat exchanger (18) is connected with the second inlet of the ring heat exchanger (18) and the lean liquid inlet of the second rich liquid pump (11) is connected with the second inlet of the lean liquid pump (18) and the second inlet of the lean liquid heat exchanger (5) is connected with the second inlet of the lean liquid pump (11), the outlet of the sulfur tail lean solution pump (13) is connected with the inlet of the sulfur tail absorption tower (7) through the sulfur tail lean solution cooler (20), the circulation interface of the sulfur tail absorption tower (5) is connected with the inlet and outlet of the reboiler (19), the reboiler (19) is connected with low-pressure steam, the exhaust end of the regeneration tower (5) is connected with the air inlet end of the regeneration gas separator (6) through the regenerated gas cooler (22), the reflux end of the regeneration gas separator (6) is connected with the reflux inlet of the regeneration tower (5) through the reflux pump (15), sulfur dioxide gas is discharged from the exhaust end of the regeneration gas separator (6), the absorption liquid distributor end of the sulfur tail absorption tower (7) is connected with the outlet of the sulfur tail recovery tank (8) through the sulfur tail recovery pump (16), the reflux end of the sulfur tail absorption tower (7) is connected with the inlet of the sulfur tail recovery tank (8), and the exhaust gas at the upper end of the sulfur tail absorption tower (7) reaches the standard.
8. A desulfurization system employing the high-efficiency sulfur dioxide absorbent according to claim 1, characterized in that: the device comprises a washing tower (1), a washing pump (9), a ring collection absorption tower (203), a rich liquid pump (204), a lean liquid heat exchanger (205), a lean liquid pump (206), a lean rich liquid heat exchanger (18), a regeneration tower (5), a reboiler (19), a regeneration gas separator (6), a reflux pump (15), a regenerated gas cooler (22), an electric demister (2) and an absorption electric demister (2014), wherein the gas inlet end of the washing tower (1) is connected with flue gas, the water inlet end of the washing tower (1) is connected with new water for production, the water outlet end of the washing tower (1) is connected with the water inlet end of the washing pump (9), the water outlet end of the washing pump (9) is simultaneously connected with a waste water discharge pipe and the water inlet end of a washing liquid distributor of the washing tower (1), the gas outlet end of the upper end of the washing tower (1) is connected with the gas inlet end of the electric demister (2), the gas outlet end of the electric demister (2) is connected with the gas inlet end of the ring collection absorption tower (203), the water outlet end of the ring collection absorption tower (203) is connected with the water inlet end of the water inlet pipe (203) of the electric demister (2), the sulfur dioxide is connected with the water inlet end of the water inlet pipe (203, the exhaust end of the absorption electric demister (2014) discharges tail gas, a first outlet of the lean-rich liquid heat exchanger (18) is connected with an inlet of the lean liquid heat exchanger (205) through the lean liquid pump (206), an outlet of the lean liquid heat exchanger (205) is connected with an upper section absorption liquid distributor end of the ring collection absorption tower (203), a liquid distributor end of the regeneration tower (5) is connected with a second outlet of the lean-rich liquid heat exchanger (18), a liquid discharge end of the regeneration tower (5) is connected with a second inlet of the lean-rich liquid heat exchanger (18), an exhaust end of the regeneration tower (5) is connected with an inlet of the regeneration gas separator (6) through the regeneration gas cooler (22), a liquid discharge end of the regeneration gas separator (6) is connected with a reflux liquid distributor end of the regeneration tower (5) through the reflux pump (15), a gas discharge end of the regeneration tower (6) discharges sulfur dioxide gas, a reboiler (5) is connected with a heating end of the regeneration gas separator (19), and the heating end of the regeneration tower (19) is connected with a low-pressure steam inlet and outlet of the regeneration gas separator (19).
9. A desulfurization system employing the high-efficiency sulfur dioxide absorbent according to claim 1, characterized in that: the device comprises a washing tower (1), a washing pump (9), an absorption tower (3), a rich liquid pump (204), a lean liquid heat exchanger (205), a lean liquid pump (206), a lean liquid heat exchanger (18), a regeneration tower (5), a reboiler (19), a regeneration gas separator (6), a reflux pump (15), a regenerated gas cooler (22), an electric demister (2), a recovery tank (3014), a recovery pump (3015) and an exhaust fan (3016), wherein the air inlet end of the washing tower (1) is connected with flue gas, the water inlet end of the washing tower (1) is connected with fresh water, the water outlet end of the washing tower (1) is connected with the water inlet end of the washing pump (9), the water outlet end of the washing pump (9) is simultaneously connected with the water inlet end of the washing tower (1) and a waste water discharge pipe, the air outlet at the upper end of the washing tower (1) is connected with the air inlet end of the electric demister (2), the air outlet end of the electric demister (2) is connected with the air inlet end of the absorption tower (3), the water outlet end of the electric demister (2) is connected with the absorption tower (3) is connected with the water inlet end of the rich liquid (9) through the water outlet end of the absorption tower (9), the sulfur dioxide is connected with the rich liquid (204) at the water outlet end of the absorption tower (18), the recovery liquid draining end of the absorption tower (3) is connected with the water inlet end of the recovery pump (3015) through the recovery tank (3014), the exhaust end of the absorption tower (3) is connected with the outlet of the lean liquid heat exchanger (205) through the exhaust fan (3016), the absorption liquid distribution end of the absorption tower (3) is connected with the inlet end of the lean liquid heat exchanger (205), the first outlet of the lean liquid heat exchanger (18) is connected with the inlet of the lean liquid heat exchanger (205) through the lean liquid pump (206), the second outlet of the lean liquid heat exchanger (18) is connected with the air inlet end of the regeneration tower (5), the liquid draining end of the regeneration tower (5) is connected with the second inlet of the lean liquid heat exchanger (18), the exhaust end of the regeneration tower (5) is connected with the air inlet end of the regeneration gas separator (6) through the regeneration gas cooler (22), the liquid draining end of the regeneration tower (6) is connected with the heating liquid distribution end of the reboiler (15), and the exhaust gas of the exhaust gas separator (19) is connected with the exhaust gas outlet end of the regeneration tower (19.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310476418.9A CN116603369A (en) | 2023-04-28 | 2023-04-28 | Absorbent capable of efficiently absorbing sulfur dioxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310476418.9A CN116603369A (en) | 2023-04-28 | 2023-04-28 | Absorbent capable of efficiently absorbing sulfur dioxide |
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| CN117547952A (en) * | 2023-12-25 | 2024-02-13 | 阳新弘盛铜业有限公司 | A method and device for purifying air quenching flue gas in copper smelting |
| CN120885034A (en) * | 2025-09-29 | 2025-11-04 | 绍兴兴欣新材料股份有限公司 | Piperazine derivative-based carbon dioxide absorbent and preparation method and application thereof |
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