CN109621638A - A kind of the deamination and desulfurization device and technique of conversion gas condensate liquid - Google Patents
A kind of the deamination and desulfurization device and technique of conversion gas condensate liquid Download PDFInfo
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- CN109621638A CN109621638A CN201811492658.3A CN201811492658A CN109621638A CN 109621638 A CN109621638 A CN 109621638A CN 201811492658 A CN201811492658 A CN 201811492658A CN 109621638 A CN109621638 A CN 109621638A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1468—Removing hydrogen sulfide
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- 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
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- 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
- B01D2252/10—Inorganic absorbents
-
- 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
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/406—Ammonia
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- 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)
- Gas Separation By Absorption (AREA)
- Industrial Gases (AREA)
Abstract
The invention discloses a kind of deamination and desulfurization device of conversion gas condensate liquid and techniques, the condensate liquid of conversion gas is delivered in stripper, steam stripped effect is heated using steam, dissolved gas in condensate liquid is parsed, the stripping gas of stripper top enters caustic wash tower, it is inversely contacted in caustic wash tower with alkaline solution, the acidic components in stripping gas are fully absorbed, and the absorbing liquid of caustic wash tower tower reactor is recycled；The stripping gas of alkali cleaning column overhead enters ammonia absorber, and water spray packing section fully absorbs the ammonia in stripping gas, and fresh water is supplemented in the bubble cap tray of Xiang Tading, absorbs a small amount of ammonia remaining in stripping gas, the inert gas emptying that top can not absorb.Ammonia absorber of the present invention is two-part, and lower section is packing material absorbing section, conducive to the cyclic absorption of ammonium hydroxide；Upper section is bubble cap tray absorber portion, and supplement fresh water absorbs micro NH in emptying end gas3, eliminate environmental pollution.
Description
Technical field
The present invention relates to a kind of deamination and desulfurization device of conversion gas condensate liquid and techniques, suitable for the condensate liquid of sulfur-bearing containing ammonia
Processing is particularly suitable for deamination and desulfurization and the recycling of the process condensate of coal chemical technology shift conversion step generation.
Background technique
In coal chemical technology, coal is generated by gasification reaction with CO, H2Based on synthesis gas, and produce a small amount of NH3、
H2S、N2Etc. foreign gases.In general, the synthesis gas from gasification reaction enters conversion section, converted CO to using conversion reaction
H2, and produced according to the difference of process route and synthesize ammonia, methanol or the unstripped gas as hydrogen peroxide, octyl alconyl etc..
In shift conversion step, because of CO and H2Conversion reaction occurs for O, therefore need to contain centainly usually from the synthesis gas of gasification process
Water-gas ratio.After the shift reaction, high temperature is generated containing wet with CO2、H2Based on conversion gas.Conversion gas is cold by cooling down step by step
But, recovery waste heat can be generated containing NH3、H2S、CO2Process condensate.Conventional process is by some processes condensate liquid
It by heating power stripper, is vented after dissolved gas is stripped, the condensate liquid after deamination and desulfurization is recycled to gasification process recycling.
Increasingly serious with Environmental Protection Situation, the drawbacks of heating power stripping mode, gradually shows, and drops a hint containing NH3、CO2、
H2S etc., directly emptying have larger peculiar smell and generate the discharge of pollutant.Numerous domestic chemical company has carried out different change to it
Into, including drop a hint and be recycled to boiler chimney, gas making gas holder and produce ammonium hydroxide etc. after cooling down.The drawbacks of these methods, is only
It is the transfer of pollutant, does not reduce the generation of pollutant fundamentally or realize resource utilization.
Summary of the invention
In order to solve the deficiencies in the prior art, the object of the present invention is to provide a kind of deamination and desulfurization of conversion gas condensate liquid dresses
It sets and technique, can effectively remove the H in conversion gas process condensate2S、NH3Deng improving the quality of condensate liquid so that condensate liquid
It can recycle, while recycle the NH in dropping a hint3, realize the resource utilization of pollutant.
To achieve the goals above, the technical solution of the present invention is as follows:
A kind of deamination and desulfurization device of conversion gas condensate liquid, including stripper, caustic wash tower and ammonia absorber, wherein stripping
The feed inlet of tower is connect with conversion gas condensate liquid source, and the top exit of stripper and the feed inlet of caustic wash tower connect, caustic wash tower
The top exit of the connection of the feed inlet of top exit and ammonia absorber, ammonia absorber connects blow-down pipe；
It include bubble-cap absorber portion and packing section inside the ammonia absorber, bubble-cap absorber portion is located at the top of packing section, steeps
Water spray system is provided between cover absorber portion and packing section, bubble-cap absorber portion is provided with bubble cap tray, bubble cap tray and water source
Connection, water source supplements fresh water into bubble cap tray, to absorb the micro NH in emptying end gas3。
First with stripper by such as NH of the dissolved gas in the process condensate in conversion gas3、H2S、CO2Deng parsing
Out, which enters in caustic wash tower, after being eluted by NaOH solution, by the H in gas2S and CO2Equal acidic components fill
Divide and absorb, subsequently into ammonia absorber, water spray is utilized to absorb the NH in stripping gas3Component.In order to fully absorb NH3Component,
It avoids causing damages to environment, two sections will be set as inside ammonia absorber, lower part is packing section, and shower water uniformly divides in packing section
Cloth, with NH3Component comes into full contact with, and most of NH in stripping gas can be absorbed3, top is bubble-cap absorber portion, into bubble cap tray
Fresh water is supplemented, to guarantee to the NH in emptying end gas3Component is fully absorbed.
Preferably, the deamination and desulfurization device further includes heat exchanger, and the cold medium of conversion gas condensate liquid source and heat exchanger is logical
The connection of road entrance, cold medium channel outlet are connect with stripper top；The thermal medium inlet of heat exchanger and the tower reactor of stripper connect
It connects, thermal medium outlet is connect with gasification process.
The conversion gas condensate liquid by waste heat recycling is preheated using the condensate liquid with higher temperature after stripping,
To guarantee Srteam Stripping effect, the consumption of outside energy is reduced.Cool down simultaneously convenient for the high-temp liquid after stripping, it is facilitated to be recycled to
Gasification process recycles.
Preferably, the entrance that the tower reactor with first circulation of the caustic wash tower pump is connect, the outlet and alkali cleaning of first circulation pump
The top of tower is connected to.
The lye of caustic wash tower tower reactor can be carried out circulated sprinkling utilization by first circulation pump.
Preferably, the bottom integrated installation of caustic wash tower cooler, cooler is multilayered structure, in the cooler
It is passed through circulating cooling liquid.Since the temperature of stripping gas is higher, when being delivered to caustic wash tower progress lye spray, it is unfavorable for lye pair
Sour gas in stripping gas is thoroughly absorbed.The integrated installation cooler in caustic wash tower, can be to being recycled back to caustic wash tower
Lye cool down, while can cool down to stripping gas, reduce the temperature of lye and stripping gas, improve lye to vapour
The absorption efficiency of sour gas in gas is proposed, harm of the sour gas to environment on the one hand can be reduced, on the other hand, can be improved
The purity for the high concentration ammonium hydroxide that washing obtains in subsequent ammonia absorber, in favor of purifying.The integrated setting of cooler simultaneously, subtracts
Lack external cooler, reduces the one-time investment of equipment.
Preferably, the tower reactor of the ammonia absorber is connected to second circulation pump inlet, and the outlet of second circulation pump and ammonia are inhaled
Receive the top connection of packing section in tower.By second circulation pump by the low concentration ammonium hydroxide circulated sprinkling of ammonia absorber tower reactor, recycle
The ammonia in stripping gas is adsorbed, on the one hand the ammonium hydroxide of available high concentration, another in order to the preparation of subsequent ammonium hydroxide product
Aspect can save the consumption of water, be conducive to resource-effective.Bubble cap tray is set in the upper section of ammonia absorber, to absorb emptying tail
Micro ammonia in gas, on the one hand can prevent that there are a small amount of ammonias to cause damages to environment in emptying end gas, on the other hand
The circulated sprinkling number that tower reactor low concentration ammonium hydroxide can be properly increased, is conducive to the ammonium hydroxide for obtaining high concentration.
A kind of deamination and desulfurization technique of conversion gas condensate liquid, includes the following steps:
The condensate liquid of conversion gas is delivered in stripper, steam stripped effect is heated using steam, by the dissolution in condensate liquid
Property gas parse, the stripping gas of stripper top enters caustic wash tower, inversely contacted in caustic wash tower with alkaline solution, strip
Acidic components in gas are fully absorbed, and the absorbing liquid of caustic wash tower tower reactor is recycled；
The stripping gas of alkali cleaning column overhead enters ammonia absorber, and water spray packing section fully absorbs the ammonia in stripping gas, to
Fresh water is supplemented in the bubble cap tray of tower top, absorbs a small amount of ammonia remaining in stripping gas, the inert gas that top can not absorb
Emptying.
Preferably, the pressure in stripper be 0.5-0.8MPa, by vacuum flashing, heating temperature raising, steam stripping side
Formula reduces ammonia nitrogen, H in condensate liquid2S content.
Preferably, the pH value in the alkali wash water of caustic wash tower is 9-11, it is ensured that the desulfurization effect of caustic wash tower.
Preferably, the absorbing liquid of caustic wash tower tower reactor is utilized by first circulation pump circulation.
Preferably, the absorbing liquid of ammonia absorber tower reactor passes through second circulation pump circulation spraying filler layer.
The invention has the benefit that
1, the present invention can solve the condensate liquid of sulphur containing ammonia in chemical plant installations in such a way that heating power stripping, alkali cleaning, ammonia absorb
Handling problems not to environmental effects, while realizing the resource utilization of pollutant.
2, feed exchanger is provided with before heating power stripper of the invention, the condensate liquid and charging sent outside using tower bottom are condensed
Liquid heat exchange, saves steam consumption.
3, caustic wash tower of the present invention is provided with NaOH solution circulating pump, and the integrated installation cooler in tower, reduces alkali liquid temperature,
Improve absorption efficiency；Setting integrated simultaneously, reduces external cooler, reduces equipment and once invest.
4, ammonia absorber of the present invention is pumped provided with ammonia circulation, is recycled and is improved ammonia concn.
5, ammonia absorber of the present invention is two-part, and lower section is packing material absorbing section, conducive to the cyclic absorption of ammonium hydroxide；Upper section is bubble
Cover tower tray absorber portion, supplement fresh water absorb micro NH in emptying end gas3, eliminate environmental pollution.
Detailed description of the invention
The accompanying drawings constituting a part of this application is used to provide further understanding of the present application, and the application's shows
Meaning property embodiment and its explanation are not constituted an undue limitation on the present application for explaining the application.
Fig. 1 is the flow diagram of present system；
Fig. 2 is the structural schematic diagram of the caustic wash tower in the present invention.
Wherein, 1, stripper, 2, caustic wash tower, 3, blow-down pipe, 4, ammonia absorber, 5, bubble-cap absorber portion, 6, packing section, 7,
First circulation pump, 8, second circulation pump, 9, heat exchanger, 10, cooler.
Specific embodiment
It is noted that described further below be all exemplary, it is intended to provide further instruction to the application.Unless another
It indicates, all technical and scientific terms used herein has usual with the application person of an ordinary skill in the technical field
The identical meanings of understanding.
It should be noted that term used herein above is merely to describe specific embodiment, and be not intended to restricted root
According to the illustrative embodiments of the application.As used herein, unless the context clearly indicates otherwise, otherwise singular
Also it is intended to include plural form, additionally, it should be understood that, when in the present specification using term "comprising" and/or " packet
Include " when, indicate existing characteristics, step, operation, device, component and/or their combination.
A kind of exemplary embodiment of the application provides a kind of deamination and desulfurization technique of condensate liquid, is applied to coal chemical industry and leads
The disposition of high ammonia nitrogen, high-sulfur condensate liquid that domain shift conversion step generates.It converts the condensate liquid generated and is delivered to heating power through valve control
Stripper heats steam stripped effect using steam, by such as NH of the dissolved gas in condensate liquid3、H2S、CO2Etc. parsing, vapour
Stripper pressure is 0.5-0.8MPa, vacuum flashing, heating temperature raising, by way of steam stripping, reduce ammonia nitrogen in condensate liquid,
H2S content.The condensate liquid parsed is recycled to gasification process；The stripping gas of stripper top enters caustic wash tower, in caustic wash tower
It is inversely contacted with NaOH solution, the H in gas2S、CO2Equal acidic components are fully absorbed, and absorbing liquid is followed by tower bottom circulating pump
Ring uses, and by control basicity, pH value etc., quantitatively supplements fresh lye, and extra raffinate is drained into sewage treatment process；Alkali
It washes top of tower gas and enters ammonia absorber, caustic wash tower pH control guarantees caustic wash tower desulfurization effect, pass through water absorption gas in 9-11
NH in body3Component, absorbing liquid are recycled by the circulating pump of tower bottom；Internal circulating load, control tower bottom ammonium hydroxide are adjusted according to demand
Concentration, and ammonium hydroxide is recycled to boiler desulfurization process, urea process, realize the utilization of resources；Tower top quantitatively supplements fresh water, top
The inert gas emptying that can not be absorbed.Process condensate sequentially enters stripper, caustic wash tower, ammonia absorber classification processing, classification
Byproduct is recycled, accomplishes that resource makes full use of.
As shown in Figure 1, the deamination and desulfurization device of conversion gas condensate liquid used in the deamination and desulfurization technique of condensate liquid, including
Stripper 1, caustic wash tower 2 and ammonia absorber 4, wherein conversion gas condensate liquid source is connect with the cold medium feeder connection of heat exchanger 9,
Cold medium channel outlet is connect with 1 top of stripper；The thermal medium inlet of heat exchanger 9 and the tower reactor of stripper connect, thermal medium
Outlet is connect with gasification process.The top exit of stripper 1 is connect with the feed inlet of caustic wash tower 2, the top exit of caustic wash tower 2 with
The feed inlet of ammonia absorber 4 connects, and the tower reactor of caustic wash tower 2 is connect with the entrance of first circulation pump 7, the outlet of first circulation pump 7
It is connected to the top of caustic wash tower 2, integrated installation cooler 10 in caustic wash tower, as shown in Fig. 2, cooler 10 is set to caustic wash tower
Bottom, cooler 10 is multilayered structure, is passed through circulating cooling liquid in cooler 10, carries out to the spray lye in caustic wash tower
Cooling, while can also cool down to stripping gas, to improve the treatment effeciency of stripping gas.Cooler 10 can be spiral knot
Structure；It may be multilayer network structure, communicated between multilayer network structure, can also be the multilayered structure of other forms.Ammonia is inhaled
The top exit for receiving tower 4 connects blow-down pipe 3.
It include bubble-cap absorber portion 5 and packing section 6 inside the ammonia absorber 4, bubble-cap absorber portion 5 is located at the upper of packing section 6
Portion, is provided with water spray system between bubble-cap absorber portion 5 and packing section 6, bubble-cap absorber portion 5 is provided with bubble cap tray, bubble column
Disk is connect with water source, and water source supplements fresh water into bubble cap tray, to absorb the micro NH in emptying end gas3.Ammonia absorber 4
Tower reactor and second circulation pump 8 inlet communications, and the outlet of second circulation pump 8 is connected to the top of packing section 6 in ammonia absorber.
First with stripper 1 by such as NH of the dissolved gas in the process condensate in conversion gas3、H2S、CO2Deng parsing
Out, which enters in caustic wash tower 2, after being eluted by NaOH solution, by the H in gas2S and CO2Equal acidic components fill
Divide and absorb, subsequently into ammonia absorber 4, water spray is utilized to absorb the NH in stripping gas3Component.In order to fully absorb NH3Group
Point, it avoids causing damages to environment, two sections will be set as inside ammonia absorber 4, lower part is packing section 6, and shower water is in packing section
It is uniformly distributed, with NH3Component comes into full contact with, and most of NH in stripping gas can be absorbed3, top is bubble-cap absorber portion 5, to bubble
Fresh water is supplemented in cover tower tray, to guarantee to the NH in emptying end gas3Component is fully absorbed.
The foregoing is merely preferred embodiment of the present application, are not intended to limit this application, for the skill of this field
For art personnel, various changes and changes are possible in this application.Within the spirit and principles of this application, made any to repair
Change, equivalent replacement, improvement etc., should be included within the scope of protection of this application.
Claims (10)
1. a kind of deamination and desulfurization device of conversion gas condensate liquid, it is characterised in that: including stripper, caustic wash tower and ammonia absorber,
Wherein, the feed inlet of stripper is connect with conversion gas condensate liquid source, and the top exit of stripper and the feed inlet of caustic wash tower connect,
The top exit of caustic wash tower and the feed inlet of ammonia absorber connect, and the top exit of ammonia absorber connects blow-down pipe；
It include bubble-cap absorber portion and packing section inside the ammonia absorber, bubble-cap absorber portion is located at the top of packing section, and bubble-cap is inhaled
It receives and is provided with water spray system between section and packing section, bubble-cap absorber portion is provided with bubble cap tray, and bubble cap tray is connect with water source,
Water source supplements fresh water into bubble cap tray, to absorb the micro NH in emptying end gas3。
2. deamination and desulfurization device according to claim 1, it is characterised in that: the deamination and desulfurization device further includes heat exchange
The cold medium feeder connection of device, conversion gas condensate liquid source and heat exchanger connects, and cold medium channel outlet is connect with stripper top；
The thermal medium inlet of heat exchanger and the tower reactor of stripper connect, and thermal medium outlet is connect with gasification process.
3. deamination and desulfurization device according to claim 1, it is characterised in that: the tower reactor and first circulation of the caustic wash tower pump
Entrance connection, first circulation pump outlet be connected to the top of caustic wash tower.
4. deamination and desulfurization device according to claim 1, it is characterised in that: alkali cleaning tower bottom integrated installation cooling
Device, cooler are multilayered structure, and circulating cooling liquid is passed through in the cooler.
5. deamination and desulfurization device according to claim 1, it is characterised in that: the tower reactor and second circulation of the ammonia absorber
The outlet of pump inlet connection, second circulation pump is connected to the top of packing section in ammonia absorber.
6. a kind of deamination and desulfurization technique of conversion gas condensate liquid, characterized by the following steps:
The condensate liquid of conversion gas is delivered in stripper, steam stripped effect is heated using steam, by the dissolubility gas in condensate liquid
Body parses, and the stripping gas of stripper top enters caustic wash tower, inversely contacts in caustic wash tower with alkaline solution, in stripping gas
Acidic components be fully absorbed, the absorbing liquid of caustic wash tower tower reactor is recycled；
The stripping gas of alkali cleaning column overhead enters ammonia absorber, and water spray packing section fully absorbs the ammonia in stripping gas, Xiang Tading
Bubble cap tray in supplement fresh water, absorb a small amount of ammonia remaining in stripping gas, the inert gas emptying that top can not absorb.
7. deamination and desulfurization technique according to claim 6, it is characterised in that: the pressure in stripper is 0.5-0.8MPa.
8. deamination and desulfurization technique according to claim 6, it is characterised in that: the pH value in the alkali wash water of caustic wash tower is 9-
11。
9. deamination and desulfurization technique according to claim 6, it is characterised in that: the absorbing liquid of caustic wash tower tower reactor is followed by first
Ring pump circulation utilizes.
10. deamination and desulfurization technique according to claim 6, it is characterised in that: the absorbing liquid of ammonia absorber tower reactor passes through the
Two circulating pump circulated sprinkling packing layers.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201811492658.3A CN109621638A (en) | 2018-12-07 | 2018-12-07 | A kind of the deamination and desulfurization device and technique of conversion gas condensate liquid |
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| CN201811492658.3A CN109621638A (en) | 2018-12-07 | 2018-12-07 | A kind of the deamination and desulfurization device and technique of conversion gas condensate liquid |
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| CN201811492658.3A Pending CN109621638A (en) | 2018-12-07 | 2018-12-07 | A kind of the deamination and desulfurization device and technique of conversion gas condensate liquid |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110133186A (en) * | 2019-04-18 | 2019-08-16 | 贵州开磷集团矿肥有限责任公司 | A kind of diammonium phosphate exhaust washer pH measuring device |
| CN115212706A (en) * | 2022-07-11 | 2022-10-21 | 江苏楷鼎环保装备有限公司 | Tail gas treatment method for sulfur black dye production system |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201091819Y (en) * | 2007-08-08 | 2008-07-30 | 山东联合化工股份有限公司 | Tail gas absorption tower for melamine united production |
| CN101664627A (en) * | 2009-09-23 | 2010-03-10 | 赢创三征（营口）精细化工有限公司 | Method and equipment for purifying tail gas generated in producing sodium cyanide by cracking light oil |
| CN201988324U (en) * | 2010-11-05 | 2011-09-28 | 合肥宁垣工程技术有限责任公司 | Multi-section combined desulfurizer |
| CN205360991U (en) * | 2016-01-18 | 2016-07-06 | 鲁丰刚 | Low boiling organic gas adsorbs treating column |
| CN106268191A (en) * | 2016-09-13 | 2017-01-04 | 中国天辰工程有限公司 | A kind of low-temperature methanol washing tail-gas water washing device and process thereof |
| CN207270896U (en) * | 2017-08-25 | 2018-04-27 | 江西艾德纳米科技有限公司 | A kind of device for absorbing tail gas |
-
2018
- 2018-12-07 CN CN201811492658.3A patent/CN109621638A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201091819Y (en) * | 2007-08-08 | 2008-07-30 | 山东联合化工股份有限公司 | Tail gas absorption tower for melamine united production |
| CN101664627A (en) * | 2009-09-23 | 2010-03-10 | 赢创三征（营口）精细化工有限公司 | Method and equipment for purifying tail gas generated in producing sodium cyanide by cracking light oil |
| CN201988324U (en) * | 2010-11-05 | 2011-09-28 | 合肥宁垣工程技术有限责任公司 | Multi-section combined desulfurizer |
| CN205360991U (en) * | 2016-01-18 | 2016-07-06 | 鲁丰刚 | Low boiling organic gas adsorbs treating column |
| CN106268191A (en) * | 2016-09-13 | 2017-01-04 | 中国天辰工程有限公司 | A kind of low-temperature methanol washing tail-gas water washing device and process thereof |
| CN207270896U (en) * | 2017-08-25 | 2018-04-27 | 江西艾德纳米科技有限公司 | A kind of device for absorbing tail gas |
Non-Patent Citations (7)
| Title |
|---|
| Z.兰特著 彭承美译: "《索尔维法制碱》", 28 February 1983, 化学工业出版社 * |
| 化学工业部人事司编: "《合成氨法制造碳酸氢铵》", 31 July 1958, 化学工业出版社 * |
| 大连化工厂，大连化工设计研究分院编: "《年产800吨合成氨厂的生产操作》", 31 March 1960, 化学工业出版社 * |
| 李小玲，曹君国: "变换冷凝液汽提系统综合改造", 《新型洁净煤技术创新与实践论文集》 * |
| 武玉婵, 蔺隆: "焦炉气18•30装置变换冷凝液处理方案探讨", 《煤化工》 * |
| 童志权，陈昭琼编: "《大气污染控制工程》", 31 October 1987, 中南工业大学出版社 * |
| 陈莉等: "一氧化碳变换冷凝液汽提工艺技术改进探讨", 《化工设计》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110133186A (en) * | 2019-04-18 | 2019-08-16 | 贵州开磷集团矿肥有限责任公司 | A kind of diammonium phosphate exhaust washer pH measuring device |
| CN115212706A (en) * | 2022-07-11 | 2022-10-21 | 江苏楷鼎环保装备有限公司 | Tail gas treatment method for sulfur black dye production system |
| CN115212706B (en) * | 2022-07-11 | 2023-08-18 | 江苏楷鼎环保装备有限公司 | Tail gas treatment method for sulfur black dye production system |
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