CN203725006U - Flue gas treatment acid absorption system - Google Patents
Flue gas treatment acid absorption system Download PDFInfo
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- CN203725006U CN203725006U CN201420053154.2U CN201420053154U CN203725006U CN 203725006 U CN203725006 U CN 203725006U CN 201420053154 U CN201420053154 U CN 201420053154U CN 203725006 U CN203725006 U CN 203725006U
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- Prior art keywords
- tower
- pipeline
- heat exchanger
- pneumatic absorbing
- quench
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- Expired - Lifetime
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 43
- 239000003546 flue gas Substances 0.000 title claims abstract description 43
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 30
- 239000002253 acid Substances 0.000 title claims abstract description 29
- 238000010791 quenching Methods 0.000 claims abstract description 48
- 239000007788 liquid Substances 0.000 claims abstract description 29
- 239000003513 alkali Substances 0.000 claims description 23
- 239000003518 caustics Substances 0.000 claims description 18
- 239000007921 spray Substances 0.000 claims description 13
- 238000003860 storage Methods 0.000 claims description 12
- 238000004140 cleaning Methods 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- 229910000975 Carbon steel Inorganic materials 0.000 claims description 3
- 239000010962 carbon steel Substances 0.000 claims description 3
- 229910002804 graphite Inorganic materials 0.000 claims description 3
- 239000010439 graphite Substances 0.000 claims description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 abstract description 32
- 238000005406 washing Methods 0.000 abstract 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 24
- 239000000243 solution Substances 0.000 description 19
- 230000009102 absorption Effects 0.000 description 16
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 12
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 12
- 238000000034 method Methods 0.000 description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 10
- 239000010881 fly ash Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 230000004087 circulation Effects 0.000 description 5
- 239000007789 gas Substances 0.000 description 3
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- JGDITNMASUZKPW-UHFFFAOYSA-K aluminium trichloride hexahydrate Chemical compound O.O.O.O.O.O.Cl[Al](Cl)Cl JGDITNMASUZKPW-UHFFFAOYSA-K 0.000 description 2
- 229940009861 aluminum chloride hexahydrate Drugs 0.000 description 2
- 229910001570 bauxite Inorganic materials 0.000 description 2
- 239000010883 coal ash Substances 0.000 description 2
- 229910052593 corundum Inorganic materials 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 235000021110 pickles Nutrition 0.000 description 2
- 229910001845 yogo sapphire Inorganic materials 0.000 description 2
- 238000010306 acid treatment Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 235000014171 carbonated beverage Nutrition 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000003020 moisturizing effect Effects 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The utility model provides a flue gas treatment acid absorption system. A quench tower is connected with a first-stage pneumatic absorption tower and a quench tower heat exchanger through pipelines; the first-stage pneumatic absorption tower is connected with a second-stage pneumatic absorption tower and a first-stage tower heat exchanger through pipelines; the second-stage pneumatic absorption tower is connected with a third-stage pneumatic absorption tower and a second-stage tower heat exchanger through pipelines; the third-stage pneumatic absorption tower is connected with an alkaline washing tower through a pipeline; the alkaline washing tower is connected with a gas-liquid separator through a pipeline; the gas-liquid separator is communicated with a chimney through a pipeline; a quench tower circulating pump is arranged on a pipeline through which the quench tower is connected with the quench tower heat exchanger; a first-stage tower circulating pump is arranged on a pipeline through which the first-stage pneumatic absorption tower is connected with the first-stage tower heat exchanger; a second-stage tower circulating pump is arranged on a pipeline through which the second-stage pneumatic absorption tower is connected with the second-stage tower heat exchanger. By the system, HCl in flue gas can be absorbed, 25-31 percent hydrochloric acid can be produced for use in plants, and flue gas can be emitted up to standard.
Description
Technical field
The utility model belongs to flue gas treating process technology, is specially containing hydrogen chloride flue gas and processes sour absorption technique system.
Background technology
Flyash is the solid waste that coal-burning power plant discharges, China Shi Yigemei TV university state, produces a large amount of aluminous fly-ash (Al2O3 >=38wt%) after coal burning, a large amount of soils are are not only occupied in the discharge of flyash, and serious environment pollution, formed the dual destruction to ecosystem environment.China is maximum in the world alumina producing state, but China's high-grade bauxite wretched insufficiency has had a strong impact on the fast development of China's aluminum oxide industry.Rationally utilize coal ash for manufacturing for aluminium oxide, both can reduce environmental pollution, can make up again the huge breach of aluminium oxide consumption, economical, societal benefits are remarkable.
For the present situation of China's bauxite resource wretched insufficiency, many scientific research institutions actively develop aluminous fly-ash comprehensive utilization and produce the research of aluminium oxide project.For the higher circulating fluid bed coal ash of activity, the normal method of direct and acid reaction that adopts is prepared aluminium oxide, and flyash acid treatment extracts aluminium oxide has become a kind of trend.Main technique tends to flyash after stripping, to generate Aluminum Chloride Hexahydrate successively through sedimentation, evaporative crystallization in hydrochloric acid, and Aluminum Chloride Hexahydrate particle resolves into aluminium oxide and hydrogen chloride gas by rotary kiln or fluiddized-bed roasting.But the subsequent treatment problem of the flue gas of the gas containing hydrogen chloride producing for roasting, does not also have clear and definite processing method at present.
Summary of the invention
The purpose of this utility model is to extract for acid system the flue gas processing problem of aluminium oxide calcining technique, provides a kind of flue gas to process sour absorption system, and it can be realized the thorough absorption of hydrogen chloride in flue gas and produce certain density hydrochloric acid is that factory is used.
Realize the technical scheme of the utility model object: a kind of flue gas is processed sour absorption system, this system comprises quench tower, one-level pneumatic absorbing tower, secondary pneumatic absorbing tower, three grades of pneumatic absorbing towers, caustic wash tower, gas-liquid separator, chimney, quench tower heat exchanger, first stage tower heat exchanger, secondary tower heat exchanger, alkali liquid tank, quench tower circulating pump, acid solution rear pump, first stage tower circulating pump, secondary tower circulating pump, three grades of tower circulating pumps, alkali cleaning circulating pump, air-introduced machine and acid solution storage tanks; Wherein, quench tower is connected by pipeline with one-level pneumatic absorbing tower and quench tower heat exchanger, one-level pneumatic absorbing tower is connected by pipeline with secondary pneumatic absorbing tower and first stage tower heat exchanger, secondary pneumatic absorbing tower is connected by pipeline with three grades of pneumatic absorbing towers and secondary tower heat exchanger, three grades of pneumatic absorbing towers are connected by pipeline with caustic wash tower, caustic wash tower is connected by pipeline with gas-liquid separator, and gas-liquid separator is connected by pipeline with chimney; On the pipeline being connected with quench tower heat exchanger at quench tower, be provided with quench tower circulating pump; On the pipeline being connected with first stage tower heat exchanger at one-level pneumatic absorbing tower, be provided with first stage tower circulating pump; On the pipeline being connected with secondary tower heat exchanger at secondary pneumatic absorbing tower, be provided with secondary tower circulating pump; Quench tower is also connected respectively acid solution storage tank with one-level pneumatic absorbing tower; Acid solution storage tank connects press filteration system by acid solution rear pump; Caustic wash tower also connects alkali liquid tank.
A kind of flue gas as above is processed sour absorption system, and the quench tower top cooling section described in it is graphite section, and hypomere is the sour tank of carbon steel line with rubber.
A kind of flue gas as above is processed sour absorption system, and the one-level pneumatic absorbing tower described in it is provided with that three layers of spray, secondary pneumatic absorbing tower are provided with two layers of spray, three grades of pneumatic absorbing towers are provided with two layers of spray.
A kind of flue gas as above is processed sour absorption system, and it is provided with three grades of tower circulating pumps on the circulated sprinkling pipeline of three grades of pneumatic absorbing towers, on the spray pipeline being connected, is provided with alkali cleaning circulating pump in alkali liquid tank outlet with caustic wash tower.
Effect of the present utility model is: the flue gas that the utility model provides is processed sour absorption system both can guarantee that the HCl in flue gas was absorbed, the hydrochloric acid that can produce 25-31% for factory simultaneously, not only can realize flue gas qualified discharge, can also, for enterprise creates certain economic benefit, there is good promotion and application prospect.
Accompanying drawing explanation
Fig. 1 is that a kind of flue gas described in the utility model is processed sour absorption system schematic diagram;
In figure: 1. quench tower; 2. one-level pneumatic absorbing tower; 3. secondary pneumatic absorbing tower; 4. three grades of pneumatic absorbing towers; 5. caustic wash tower; 6. gas-liquid separator; 7. chimney; 8. quench tower heat exchanger; 9. first stage tower heat exchanger; 10. secondary tower heat exchanger; 11. alkali liquid tanks; 12. quench tower circulating pumps; 13. acid solution rear pumps; 14. first stage tower circulating pumps; 15. secondary tower circulating pumps; 16. 3 grades of tower circulating pumps; 17. alkali cleaning circulating pumps; 18. air-introduced machines; 19. acid solution storage tanks.
The specific embodiment
Below in conjunction with the drawings and specific embodiments, a kind of flue gas described in the utility model being processed to sour absorption system is further described.
As shown in Figure 1, a kind of flue gas described in the utility model is processed sour absorption system and is comprised quench tower 1, one-level pneumatic absorbing tower 2, secondary pneumatic absorbing tower 3, three grades of pneumatic absorbing towers 4, caustic wash tower 5, gas-liquid separator 6, chimney 7, quench tower heat exchanger 8, first stage tower heat exchanger 9, secondary tower heat exchanger 10, alkali liquid tank 11, quench tower circulating pump 12, acid solution rear pump 13, first stage tower circulating pump 14, secondary tower circulating pump 15, three grades of tower circulating pumps 16, alkali cleaning circulating pump 17, air-introduced machine 18 and acid solution storage tanks 19;
Wherein, quench tower 1 is connected by pipeline with one-level pneumatic absorbing tower 2 and quench tower heat exchanger 8, one-level pneumatic absorbing tower 2 is connected by pipeline with secondary pneumatic absorbing tower 3 and first stage tower heat exchanger 9, secondary pneumatic absorbing tower 3 is connected by pipeline with three grades of pneumatic absorbing towers 4 and secondary tower heat exchanger 10, three grades of pneumatic absorbing towers 4 are connected by pipeline with caustic wash tower 5, caustic wash tower 5 is connected by pipeline with gas-liquid separator 6, and gas-liquid separator 6 is connected by pipeline with chimney 7;
On the pipeline being connected with quench tower heat exchanger 8 at quench tower 1, be provided with quench tower circulating pump 12; On the pipeline being connected with first stage tower heat exchanger 9 at one-level pneumatic absorbing tower 2, be provided with first stage tower circulating pump 14; On the pipeline being connected with secondary tower heat exchanger 10 at secondary pneumatic absorbing tower 3, be provided with secondary tower circulating pump 15; Quench tower 1 is also connected respectively acid solution storage tank 19 with one-level pneumatic absorbing tower 2; Acid solution storage tank 19 connects press filteration system by acid solution rear pump 13; Caustic wash tower 5 also connects alkali liquid tank 11.
Described quench tower 1 top cooling section is graphite section, and hypomere is the sour tank of carbon steel line with rubber.
Described one-level pneumatic absorbing tower 2 is provided with that three layers of spray, secondary pneumatic absorbing tower 3 are provided with two layers of spray, three grades of pneumatic absorbing towers 4 are provided with two layers of spray.
On the circulated sprinkling pipeline of three grades of pneumatic absorbing towers 4, be provided with three grades of tower circulating pumps 16, on the spray pipeline being connected with caustic wash tower 5 in alkali liquid tank 11 outlets, be provided with alkali cleaning circulating pump 17.
Adopting a kind of flue gas of system described in the utility model to process sour absorption process comprises the steps:
(a) flue gas after aluminium chloride roasting system is processed enters quench tower 1, in quench tower 1, flue gas directly contact with the circulation watery hydrochloric acid following current of atomisation conduct heat, mass transport process; Gained acid solution is sent into quench tower heat exchanger 8 and recirculated cooling water contact heat-exchanging by quench tower circulating pump 12, from quench tower 1 acid liquor temperature out, be 60～80 ℃ (for example 60 ℃, 70 ℃ or 80 ℃), after quench tower heat exchanger 8 cools to approximately 50 ℃, send back to quench tower 1; For assurance flue gas, lower the temperature smoothly, industry water moisturizing is set, after chilling, flue-gas temperature is reduced to 60～80 ℃ (for example 60 ℃, 70 ℃ or 80 ℃); In quench tower 1, there is a small amount of HCl to be absorbed, after reaching finite concentration, the watery hydrochloric acid circulation of generation enters acid solution storage tank 19.In the first product acid that quench tower 1 and one-level pneumatic absorbing tower 2 produce, contain the Al2O3 impurity that roasting produces, by acid solution rear pump 13, be sent to after press filteration system press filtration, purer filtrate is sent factory back to and is continued to use.
(b) flue gas after quench tower 1 cooling enters one-level pneumatic absorbing tower 2, and in one-level pneumatic absorbing tower 2, cigarette G&W fully contacts, and water absorbs the HCl in flue gas, forms dilute hydrochloric acid solution; Dilute hydrochloric acid solution is stored in tower bottom, then sends into first stage tower heat exchanger 9 by first stage tower circulating pump 14, is reduced to 30 ℃ sprays into one-level pneumatic absorbing tower 2 and recycle with temperature after chilled water heat exchange; When reaching 25～31%, concentration passes out to acid solution storage tank 19; After one-level pneumatic absorbing tower 2, flue-gas temperature is reduced to approximately 40 ℃ and enters into secondary pneumatic absorbing tower 3;
(c) in secondary pneumatic absorbing tower 3, flue gas absorbs dilute hydrochloric acid liquid with circulation and goes in the same direction, and now, the HCl gas dissolution in flue gas is in pickle, and water vapour is condensed into water; Pickle is sent back in tower in secondary tower heat exchanger 10 Yu after chilled water heat exchange via secondary circulating pump 15; By secondary pneumatic absorbing tower 3 bottoms hydrochloric acid out, a part is transmitted back to one-level pneumatic absorbing tower 2, in the interior circulation of one-level pneumatic absorbing tower 2, absorbs enrichment, and all the other major parts are by sour pumped back secondary pneumatic absorbing tower 3, as the absorption liquid of secondary pneumatic absorbing tower 3;
(d) from secondary pneumatic absorbing tower 3 flue gas out, its HCl content reduces greatly, enters into three grades of pneumatic absorbing towers 4; In three grades of pneumatic absorbing towers 4, flue gas fully contacts with cooling rear acid solution, and the HCl in flue gas is absorbed, and absorption liquid stores up acid section under tower, by three grades of tower circulating pump 16 parts, deliver to secondary pneumatic absorbing tower 3 again and carry out enrichment, another part is transmitted back to 4 circulations of three grades of pneumatic absorbing towers; After three grades of pneumatic absorbing towers, the HCl in flue gas is absorbed approximately 99.5%.
(e) flue gas after three grades of absorptions enters into caustic wash tower 5, and in caustic wash tower 5, flue gas goes in the same direction with the alkali lye from alkali cleaning circulating pump 17, haptoreaction, and in flue gas, remaining few HCl is neutralized by the NaOH in alkali lye; Liquid self-flowing after neutralization is got back in alkali liquid tank 11; Through the pH value in detecting alkali liquid tank, in tank, supplement the NaOH aqueous solution or the salt solution after neutralization is sent to battery limit (BL);
(f) flue gas after alkali cleaning is undertaken, after carbonated drink separation, through air-introduced machine 18, sending chimney 7 by gas-liquid separator 6, and fume emission is up to state standards.
Watery hydrochloric acid concentration described above is below 25%.
Claims (4)
1. a flue gas is processed sour absorption system, it is characterized in that: this system comprises quench tower (1), one-level pneumatic absorbing tower (2), secondary pneumatic absorbing tower (3), three grades of pneumatic absorbing towers (4), caustic wash tower (5), gas-liquid separator (6), chimney (7), quench tower heat exchanger (8), first stage tower heat exchanger (9), secondary tower heat exchanger (10), alkali liquid tank (11), quench tower circulating pump (12), acid solution rear pump (13), first stage tower circulating pump (14), secondary tower circulating pump (15), three grades of tower circulating pumps (16), alkali cleaning circulating pump (17), air-introduced machine (18) and acid solution storage tank (19),
Wherein, quench tower (1) is connected by pipeline with one-level pneumatic absorbing tower (2) and quench tower heat exchanger (8), one-level pneumatic absorbing tower (2) is connected by pipeline with secondary pneumatic absorbing tower (3) and first stage tower heat exchanger (9), secondary pneumatic absorbing tower (3) is connected by pipeline with three grades of pneumatic absorbing towers (4) and secondary tower heat exchanger (10), three grades of pneumatic absorbing towers (4) are connected by pipeline with caustic wash tower (5), caustic wash tower (5) is connected by pipeline with gas-liquid separator (6), and gas-liquid separator (6) is connected by pipeline with chimney (7);
On the pipeline being connected with quench tower heat exchanger (8) at quench tower (1), be provided with quench tower circulating pump (12); On the pipeline being connected with first stage tower heat exchanger (9) at one-level pneumatic absorbing tower (2), be provided with first stage tower circulating pump (14); On the pipeline being connected with secondary tower heat exchanger (10) at secondary pneumatic absorbing tower (3), be provided with secondary tower circulating pump (15); Quench tower (1) is also connected respectively acid solution storage tank (19) with one-level pneumatic absorbing tower (2); Acid solution storage tank (19) connects press filteration system by acid solution rear pump (13); Caustic wash tower (5) also connects alkali liquid tank (11).
2. a kind of flue gas according to claim 1 is processed sour absorption system, it is characterized in that, described quench tower (1) top cooling section is graphite section, and hypomere is the sour tank of carbon steel line with rubber.
3. a kind of flue gas according to claim 1 is processed sour absorption system, it is characterized in that, described one-level pneumatic absorbing tower (2) is provided with that three layers of spray, secondary pneumatic absorbing tower (3) are provided with two layers of spray, three grades of pneumatic absorbing towers (4) are provided with two layers of spray.
4. a kind of flue gas according to claim 1 is processed sour absorption system, it is characterized in that, on the circulated sprinkling pipeline of three grades of pneumatic absorbing towers (4), be provided with three grades of tower circulating pumps (16), on the spray pipeline being connected with caustic wash tower (5) in alkali liquid tank (11) outlet, be provided with alkali cleaning circulating pump (17).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420053154.2U CN203725006U (en) | 2014-01-27 | 2014-01-27 | Flue gas treatment acid absorption system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420053154.2U CN203725006U (en) | 2014-01-27 | 2014-01-27 | Flue gas treatment acid absorption system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203725006U true CN203725006U (en) | 2014-07-23 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420053154.2U Expired - Lifetime CN203725006U (en) | 2014-01-27 | 2014-01-27 | Flue gas treatment acid absorption system |
Country Status (1)
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| CN (1) | CN203725006U (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103752159A (en) * | 2014-01-27 | 2014-04-30 | 北京航天动力研究所 | Flue gas treatment acid absorption system and method |
| CN104474864A (en) * | 2014-11-14 | 2015-04-01 | 江西铜业股份有限公司 | New hydrogen sulfide absorption system |
| CN105937765A (en) * | 2016-06-08 | 2016-09-14 | 北京航天动力研究所 | Incinerating quenching device used for treatment of high-viscosity and strong-corrosive salt containing waste liquid and incinerating quenching method used for treatment of high viscosity and strong corrosive salt containing waste liquid |
| CN106422680A (en) * | 2016-11-22 | 2017-02-22 | 杭州东日节能技术有限公司 | Smelting off-gas purification treatment device and method capable of producing by-product sulfuric acid with the concentration being 40% or higher |
| CN108926982A (en) * | 2017-05-25 | 2018-12-04 | 新特能源股份有限公司 | The device and method of separating hydrogen chloride from tail gas in production of gas-phase silica |
| CN112044237A (en) * | 2019-06-06 | 2020-12-08 | Cmi优威克股份有限公司 | System, method for cleaning a flue gas comprising an acid component, and/or for regenerating an acid component comprised in a flue gas |
| US11376546B2 (en) | 2018-09-24 | 2022-07-05 | Valmet Technologies Oy | Method and a system for producing hydrochloric acid from flue gases |
-
2014
- 2014-01-27 CN CN201420053154.2U patent/CN203725006U/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103752159A (en) * | 2014-01-27 | 2014-04-30 | 北京航天动力研究所 | Flue gas treatment acid absorption system and method |
| CN104474864A (en) * | 2014-11-14 | 2015-04-01 | 江西铜业股份有限公司 | New hydrogen sulfide absorption system |
| CN105937765A (en) * | 2016-06-08 | 2016-09-14 | 北京航天动力研究所 | Incinerating quenching device used for treatment of high-viscosity and strong-corrosive salt containing waste liquid and incinerating quenching method used for treatment of high viscosity and strong corrosive salt containing waste liquid |
| CN106422680A (en) * | 2016-11-22 | 2017-02-22 | 杭州东日节能技术有限公司 | Smelting off-gas purification treatment device and method capable of producing by-product sulfuric acid with the concentration being 40% or higher |
| CN106422680B (en) * | 2016-11-22 | 2022-09-09 | 杭州东日节能技术有限公司 | Smelting flue gas purification treatment device and method with byproduct sulfuric acid of more than 40% |
| CN108926982A (en) * | 2017-05-25 | 2018-12-04 | 新特能源股份有限公司 | The device and method of separating hydrogen chloride from tail gas in production of gas-phase silica |
| US11376546B2 (en) | 2018-09-24 | 2022-07-05 | Valmet Technologies Oy | Method and a system for producing hydrochloric acid from flue gases |
| CN112044237A (en) * | 2019-06-06 | 2020-12-08 | Cmi优威克股份有限公司 | System, method for cleaning a flue gas comprising an acid component, and/or for regenerating an acid component comprised in a flue gas |
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Legal Events
| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170204 Address after: 100076 Beijing, Fengtai District, South Road, No. 1, Patentee after: BEIJING AEROSPACE PETROCHEMICAL TECHNOLOGY & EQUIPMENT ENGINEERING Corp.,Ltd. Address before: 100076 Beijing, Fengtai District, South Road, No. 1, Patentee before: BEIJING AEROSPACE PROPULSION INSTITUTE |
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| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170322 Address after: 100076 Beijing, Fengtai District, South Road, No. 1, Patentee after: Beijing wing wing Technology Co.,Ltd. Address before: 100076 Beijing, Fengtai District, South Road, No. 1, Patentee before: BEIJING AEROSPACE PETROCHEMICAL TECHNOLOGY & EQUIPMENT ENGINEERING Corp.,Ltd. |
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| CP01 | Change in the name or title of a patent holder | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 100076 Beijing, Fengtai District, South Road, No. 1, Patentee after: BEIJING HANGHUA ENERGY SAVING AND ENVIRONMENTAL PROTECTION TECHNOLOGY CO.,LTD. Address before: 100076 Beijing, Fengtai District, South Road, No. 1, Patentee before: Beijing wing wing Technology Co.,Ltd. |
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| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20140723 |