CN108100996A - The processing system and method for by-product HCl in continuity method production processes of chloroacetic acid - Google Patents
The processing system and method for by-product HCl in continuity method production processes of chloroacetic acid Download PDFInfo
- Publication number
- CN108100996A CN108100996A CN201810149848.9A CN201810149848A CN108100996A CN 108100996 A CN108100996 A CN 108100996A CN 201810149848 A CN201810149848 A CN 201810149848A CN 108100996 A CN108100996 A CN 108100996A
- Authority
- CN
- China
- Prior art keywords
- hcl
- chlorine
- gas
- synthetic furnace
- processing system
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 22
- 239000006227 byproduct Substances 0.000 title claims abstract description 20
- FOCAUTSVDIKZOP-UHFFFAOYSA-N chloroacetic acid Chemical compound OC(=O)CCl FOCAUTSVDIKZOP-UHFFFAOYSA-N 0.000 title claims abstract description 15
- 229940106681 chloroacetic acid Drugs 0.000 title claims abstract description 14
- 239000007789 gas Substances 0.000 claims abstract description 61
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 57
- 239000000460 chlorine Substances 0.000 claims abstract description 57
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 57
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000001257 hydrogen Substances 0.000 claims abstract description 37
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 37
- 238000005660 chlorination reaction Methods 0.000 claims abstract description 33
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 claims abstract description 13
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 13
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 13
- 238000003672 processing method Methods 0.000 claims abstract description 11
- 239000000178 monomer Substances 0.000 claims abstract description 8
- 238000000746 purification Methods 0.000 claims abstract description 8
- WFDIJRYMOXRFFG-UHFFFAOYSA-N Acetic anhydride Chemical compound CC(=O)OC(C)=O WFDIJRYMOXRFFG-UHFFFAOYSA-N 0.000 claims description 24
- 239000012535 impurity Substances 0.000 claims description 11
- 239000003054 catalyst Substances 0.000 claims description 8
- 239000007791 liquid phase Substances 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- -1 gas condenser Chemical compound 0.000 claims description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- 229910002804 graphite Inorganic materials 0.000 claims description 3
- 239000010439 graphite Substances 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 3
- 230000003139 buffering effect Effects 0.000 claims description 2
- 239000012071 phase Substances 0.000 claims 1
- 239000002699 waste material Substances 0.000 abstract description 4
- 239000003513 alkali Substances 0.000 abstract description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 54
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 21
- FDRCDNZGSXJAFP-UHFFFAOYSA-M sodium chloroacetate Chemical compound [Na+].[O-]C(=O)CCl FDRCDNZGSXJAFP-UHFFFAOYSA-M 0.000 description 7
- VGCXGMAHQTYDJK-UHFFFAOYSA-N Chloroacetyl chloride Chemical compound ClCC(Cl)=O VGCXGMAHQTYDJK-UHFFFAOYSA-N 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000010453 quartz Substances 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 238000002156 mixing Methods 0.000 description 3
- DHMQDGOQFOQNFH-UHFFFAOYSA-N Glycine Chemical compound NCC(O)=O DHMQDGOQFOQNFH-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 229920002134 Carboxymethyl cellulose Polymers 0.000 description 1
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- 239000004471 Glycine Substances 0.000 description 1
- 238000010923 batch production Methods 0.000 description 1
- 239000001768 carboxy methyl cellulose Substances 0.000 description 1
- 235000010948 carboxy methyl cellulose Nutrition 0.000 description 1
- 239000008112 carboxymethyl-cellulose Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000007809 chemical reaction catalyst Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to the processing systems and method of by-product HCl in the processing system and processing method of HCl, particularly a kind of continuity method production processes of chloroacetic acid.Processing system includes gas condenser, and surge tank, chlorine hydrogen synthetic furnace, gas condenser is connected with the gas outlet on chlorination tank, and condensator outlet is connected with HCl surge tanks, is connected after the pure chlorine pipeline of HCl surge tanks outlet conduit access with chlorine hydrogen synthetic furnace.Processing method：Tail gas condenses purifying and is passed through chlorine hydrogen synthetic furnace with the later stage and mixes in advance burns purifying, and the HCl after final purification is used for the synthesis of vinyl chloride monomer.HCl tail gas is carried out after condensing purification processes in advance, then the HCl tail gas containing chlorine is passed through chlorine hydrogen synthetic furnace and mixes burning, the chlorine in HCl is removed, by-product HCl is made to can be used in the synthesis of chlor-alkali enterprises vinyl chloride monomer, achievees the purpose that waste utilization.
Description
Technical field
The present invention relates to secondary in the processing system and processing method of HCl, particularly a kind of continuity method production processes of chloroacetic acid
Produce the processing system and method for HCl.
Background technology
Monoxone is a kind of important Organic Chemicals, is mainly used to produce carboxymethyl cellulose, glycine, monoxone
Ethyl ester etc..The chloroacetic main method of industrialized production is acetic acid catalytic chlorination process at present, it is specific can be divided into again continuity method and
It has a rest method.Continuity method is compared with batch process, with unit scale is small, production capacity is big, production technology is advanced, product quality is high, pollution is rotten
The advantages that erosion is few.
Acetic acid chlorination can generate a large amount of HCl tail gas, and continuity method monoxone technique is using aceticanhydride as catalyst, by acetic acid through chlorine
Gas chlorination reaction generates, and is removed in tail gas containing a large amount of HCl, also containing a small amount of chlorine, chloroacetic chloride, acetic acid, monoxone.It is given birth in monoxone
In production, tail gas water is generally absorbed into production hydrochloric acid, as byproduct.But since such hydrochloric acid purity is low, poor quality, contain
Have the organic matters such as monoxone, acetic acid, free chlorine contents are exceeded, cause application field critical constraints, there are no it is economical, have and can grasp
The harmlessness disposing approach for the property made.
The content of the invention
The goal of the invention of the present invention is the deficiency for overcoming the prior art and provides a kind of continuity method production processes of chloroacetic acid
The processing system and method for middle by-product HCl.
The processing system of the present invention adopts the following technical scheme that：
The processing system that by-product HCl is recycled in a kind of continuity method production processes of chloroacetic acid, including gas condenser, surge tank,
Chlorine hydrogen synthetic furnace, gas condenser are connected with the gas outlet on chlorination tank, and condensator outlet is connected with HCl surge tanks, HCl bufferings
Tank outlet conduit is connected after accessing pure chlorine pipeline with chlorine hydrogen synthetic furnace.
Technical solution used by the processing system compared with prior art, can remove the chlorine in HCl, make by-product
HCl can be used in the synthesis of chlor-alkali enterprises vinyl chloride monomer, achieve the purpose that waste utilization.
The preferred embodiment of the processing system is：
Chlorine hydrogen synthetic furnace is also connected by pipeline with hydrogen water trap.
Gas condenser is connected by pumping with chlorination tank.
Gas condenser uses graphite condenser.
Processing method the technical solution adopted is that：
The processing method that by-product HCl is recycled in a kind of continuity method production processes of chloroacetic acid, tail gas condense purifying and later stage in advance
It is passed through chlorine hydrogen synthetic furnace and mixes and burn purifying, the HCl after final purification is used for the synthesis of vinyl chloride monomer.
The invention has the advantages and positive effects that：1. realize the waste utilization of by-product HCl gases；2. it reduces low-quality
The generation of by-product hydrochloric acid reduces pure water consumption；3. the chlorination reaction catalyst being mixed in tail gas, intermediate product foldback are returned into chlorination
Kettle reduces the consumption of catalyst aceticanhydride, reduces production cost.
Processing method use preferred embodiment be：
Mixed tail gas after chlorination enters gas condenser by chlorination tank, the extra organic matter being condensed out at -20 ~ -30 DEG C
Impurity returns to chlorination tank with liquid phase, then the HCl condensation tail gas for being mixed with chlorine is sent into HCl surge tanks, is mixed afterwards with chlorine, into
Enter chlorine hydrogen synthetic furnace；The HCl gases without free chlorine are made, for VCM synthesis.
Mixed gas is with hydrogen according to 1:1.05 ~ 1.2 volume ratios are mixed into chlorine hydrogen synthetic furnace and mix burning.
Liquid phase mixture containing organic impurities is returned to chlorination tank, for chlorination reaction, reduces catalyst aceticanhydride and disappears
Consumption mass ratio 5.2 ~ 6.1%.
Description of the drawings
Fig. 1 is the structure diagram of the present invention.
Specific embodiment
The present invention is described in detail with reference to the accompanying drawings and embodiments：
The processing system that by-product HCl is recycled in a kind of continuity method production processes of chloroacetic acid, referring to attached drawing 1, in figure：Chlorination tank 1,
Gas condenser 2, HCl surge tanks 3, Chlorine Buffer Vessel 4, hydrogen water trap 5, chlorine hydrogen synthetic furnace 6.
In present treatment system, gas condenser 2 is connected with the gas outlet on chlorination tank 1, and gas condenser 1 exports and HCl
Surge tank 3 connects, and is synthesized after the pure chlorine pipeline that the access of 3 outlet conduit of HCl surge tanks is connected with Chlorine Buffer Vessel 4 with chlorine hydrogen
Stove 6 connects.
Chlorine hydrogen synthetic furnace 6 is also connected by pipeline with hydrogen water trap 5；Gas condenser 2 is connected by pumping with chlorination tank 1
It connects.
Gas condenser 1 uses graphite condenser；
Tail gas is passed through chlorine hydrogen synthetic furnace 6 and mixes and burn purifying through condensing purifying and later stage in advance, and the HCl after final purification is used for vinyl chloride
The synthesis of monomer.
Mixed tail gas after chlorination enters gas condenser 2 by chlorination tank 1, and what is be condensed out at -20 ~ -30 DEG C is extra
Organic impurities（Organic impurities include a small amount of monoxone, chloroacetic chloride and acetic acid）It is returned with liquid phase in chlorination tank 1, then will be mixed
The HCl condensation tail gas for having chlorine is sent into HCl surge tanks 3, is mixed afterwards with the chlorine supplied in Chlorine Buffer Vessel 4, gaseous mixture
Body is with hydrogen according to 1:1.05 ~ 1.2 volume ratios, into chlorine hydrogen synthetic furnace 6；The HCl gases without free chlorine are made, for chloroethene
Alkene synthesizes.
Liquid phase mixture containing organic impurities is returned to chlorination tank, for chlorination reaction, reduces catalyst aceticanhydride and disappears
Consumption 5.2 ~ 6.1%（Mass percent）.
Above-mentioned processing method compared with prior art, HCl tail gas is carried out after condensing purification processes in advance, then will contain chlorine
HCl tail gas be passed through chlorine hydrogen synthetic furnace and mix burning, remove the chlorine in HCl, by-product HCl made to can be used in chlor-alkali enterprises vinyl chloride list
The synthesis of body, achievees the purpose that waste utilization.
Embodiment 1：
A kind of method that by-product HCl tail gas refines recycling in production processes of chloroacetic acid, after superchlorination, tail gas mixed gas
（Volume ratio：Containing HCl 95%, chlorine 1%, chloroacetic chloride 1.2%, other gases account for 2.8%）It enters in gas condenser 2, by-
30 DEG C of condensations remove chloroacetic chloride and other impurities in mixed gas, and this liquid phase mixture foldback are returned chlorination tank 1, make it
Chlorination reaction is back to, reduces catalyst aceticanhydride consumption about 6.1%（Mass percent）, the HCl impurity condensed after purification is main
For chlorine（1% volume ratio）, with chlorine with 1 after HCl surge tanks 3:10 volume ratio mixing, afterwards into chlorine hydrogen synthetic furnace 6
Quartz lamp head middle level, hydrogen enter the inside and outside layer of quartz lamp head, burn on lamp cap top, into the mixed gas of chlorine hydrogen synthetic furnace,
（HCl+ chlorine）:Hydrogen=1:1.05, HCl is synthesized, reaction process is stablized, and HCl comes out of the stove purity 95.5% after reaction, is sent into vinyl chloride
Monomer synthesis device is used for the synthesis of vinyl chloride.
Embodiment 2：
A kind of method that by-product HCl tail gas refines recycling in production processes of chloroacetic acid, after superchlorination, tail gas mixed gas
（Volume ratio：Containing HCl 93%, chlorine 1.5%, chloroacetic chloride 1%, other gases account for 4.5%）It enters in gas condenser 2, by-
20 DEG C of condensations remove chloroacetic chloride and other impurities in mixed gas, and this liquid phase mixture foldback are returned chlorination tank 1, make it
Chlorination reaction is back to, reduces catalyst aceticanhydride consumption about 5.2%（Mass percent）, the HCl impurity condensed after purification is main
For chlorine（1.5% volume ratio）, with chlorine with 0.5 after HCl surge tanks 3:10 volume ratio mixing, synthesizes afterwards into chlorine hydrogen
The quartz lamp head middle level of stove 6, hydrogen enter the inside and outside layer of quartz lamp head, burn on lamp cap top, into the mixing of chlorine hydrogen synthetic furnace
Gas,（HCl+ chlorine）:Hydrogen=1:1.2, HCl is synthesized, reaction process is stablized, and HCl comes out of the stove purity 96% after reaction, is sent into chloroethene
Alkene monomer synthesis device is used for the synthesis of vinyl chloride.
Of the invention to be sold with traditional absorbed with water outside generation hydrochloric acid, ton production monoxone can reduce by about 1.03 tons of low-quality hydrochloric acid
（By 31% densimeter）Generation, while 0.71 ton of fresh water consumption can be saved；Method using the present invention, byproduct HCl can
Vinyl chloride production is completely used for, while Condensate reuse reduces catalyst aceticanhydride consumption in acetic acid chlorination reaction.
Claims (8)
1. a kind of processing system that by-product HCl is recycled in continuity method production processes of chloroacetic acid, including gas condenser, buffering
Tank, chlorine hydrogen synthetic furnace, it is characterised in that：Gas condenser is connected with the gas outlet on chlorination tank, gas condenser outlet and HCl
Surge tank connects, and HCl surge tanks outlet conduit is connected after accessing pure chlorine pipeline with chlorine hydrogen synthetic furnace.
2. the processing system that by-product HCl is recycled in continuity method production processes of chloroacetic acid according to claim 1, feature
It is：Chlorine hydrogen synthetic furnace is also connected by pipeline with hydrogen water trap.
3. the processing system that by-product HCl is recycled in continuity method production processes of chloroacetic acid according to claim 1, feature
It is：Gas condenser is connected by pumping with chlorination tank.
4. the processing system that by-product HCl is recycled in continuity method production processes of chloroacetic acid according to claim 1, feature
It is：Gas condenser uses graphite condenser.
5. a kind of processing method of processing system as described in any one in Claims 1-4, it is characterised in that：Tail gas is first
Phase condensation purifying is passed through chlorine hydrogen synthetic furnace and mixes with the later stage burns purifying, and the HCl after final purification is used for the synthesis of vinyl chloride monomer.
6. processing method according to claim 5, it is characterised in that：Mixed tail gas after chlorination enters gas by chlorination tank
Condenser, the extra organic impurities being condensed out at -20 ~ -30 DEG C return to chlorination tank with liquid phase, then will be mixed with chlorine
HCl condensation tail gas is sent into HCl surge tanks, is mixed afterwards with chlorine, into chlorine hydrogen synthetic furnace；The HCl gas without free chlorine is made
Body, for VCM synthesis.
7. processing method according to claim 6, it is characterised in that：Mixed gas is with hydrogen according to 1:1.05 ~ 1.2 volumes
Burning is mixed than being mixed into chlorine hydrogen synthetic furnace.
8. processing method according to claim 6, it is characterised in that：Liquid phase mixture containing organic impurities is returned to
Chlorination tank for chlorination reaction, reduces catalyst aceticanhydride consumption mass ratio 5.2 ~ 6.1%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810149848.9A CN108100996A (en) | 2018-02-13 | 2018-02-13 | The processing system and method for by-product HCl in continuity method production processes of chloroacetic acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810149848.9A CN108100996A (en) | 2018-02-13 | 2018-02-13 | The processing system and method for by-product HCl in continuity method production processes of chloroacetic acid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108100996A true CN108100996A (en) | 2018-06-01 |
Family
ID=62205905
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810149848.9A Pending CN108100996A (en) | 2018-02-13 | 2018-02-13 | The processing system and method for by-product HCl in continuity method production processes of chloroacetic acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108100996A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110057820A (en) * | 2019-04-15 | 2019-07-26 | 中南大学 | Method, system and the storage medium of on-line checking hydrogen chloride synthetic furnace chlorine hydrogen proportion |
| CN112010731A (en) * | 2020-09-14 | 2020-12-01 | 河南神马氯碱发展有限责任公司 | Method and device for preparing chloroethylene by treating bis (trichloromethyl) carbonate production tail gas through catalytic chlorination method |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB695063A (en) * | 1951-05-11 | 1953-08-05 | Ici Ltd | Improvements in or relating to the purification of hydrogen chloride |
| CN101274195A (en) * | 2007-12-24 | 2008-10-01 | 天津大学 | Method for removing residual chlorine gas in tail gas in production processes of chloroacetic acid |
| CN104649887A (en) * | 2015-02-05 | 2015-05-27 | 中国天辰工程有限公司 | Production method of chloroacetic acid and method for recovering catalysts in production process of chloroacetic acid |
| CN105060249A (en) * | 2015-07-28 | 2015-11-18 | 江苏同泰化工有限公司 | Method for preparing refined hydrochloric acid by using tail gas hydrogen chloride produced in chloroacetic acid production |
| CN106220491A (en) * | 2016-07-29 | 2016-12-14 | 河北科技大学 | Production of chloroacetic acid method |
| CN107108438A (en) * | 2015-10-13 | 2017-08-29 | 阿克苏诺贝尔化学品国际有限公司 | The method for preparing monochloro acetic acid |
| CN208054910U (en) * | 2018-02-13 | 2018-11-06 | 唐山三友氯碱有限责任公司 | The processing system of by-product HCl in continuity method production processes of chloroacetic acid |
-
2018
- 2018-02-13 CN CN201810149848.9A patent/CN108100996A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB695063A (en) * | 1951-05-11 | 1953-08-05 | Ici Ltd | Improvements in or relating to the purification of hydrogen chloride |
| CN101274195A (en) * | 2007-12-24 | 2008-10-01 | 天津大学 | Method for removing residual chlorine gas in tail gas in production processes of chloroacetic acid |
| CN104649887A (en) * | 2015-02-05 | 2015-05-27 | 中国天辰工程有限公司 | Production method of chloroacetic acid and method for recovering catalysts in production process of chloroacetic acid |
| CN105060249A (en) * | 2015-07-28 | 2015-11-18 | 江苏同泰化工有限公司 | Method for preparing refined hydrochloric acid by using tail gas hydrogen chloride produced in chloroacetic acid production |
| CN107108438A (en) * | 2015-10-13 | 2017-08-29 | 阿克苏诺贝尔化学品国际有限公司 | The method for preparing monochloro acetic acid |
| CN106220491A (en) * | 2016-07-29 | 2016-12-14 | 河北科技大学 | Production of chloroacetic acid method |
| CN208054910U (en) * | 2018-02-13 | 2018-11-06 | 唐山三友氯碱有限责任公司 | The processing system of by-product HCl in continuity method production processes of chloroacetic acid |
Non-Patent Citations (2)
| Title |
|---|
| 程祖球等: "《化工基础》", 化学工业出版社, pages: 558 * |
| 高大力, 王传玲, 辛衍刚: "简述氯乙酸尾气的处理方法", 中国氯碱, no. 03, pages 37 - 38 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110057820A (en) * | 2019-04-15 | 2019-07-26 | 中南大学 | Method, system and the storage medium of on-line checking hydrogen chloride synthetic furnace chlorine hydrogen proportion |
| CN110057820B (en) * | 2019-04-15 | 2021-04-30 | 中南大学 | Method, system and storage medium for on-line detection of chlorine-hydrogen ratio of hydrogen chloride synthesis furnace |
| CN112010731A (en) * | 2020-09-14 | 2020-12-01 | 河南神马氯碱发展有限责任公司 | Method and device for preparing chloroethylene by treating bis (trichloromethyl) carbonate production tail gas through catalytic chlorination method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1865127A (en) | Separation and purification method of mixed waste gas containing chlorine and hydrogen chloride | |
| CN108100996A (en) | The processing system and method for by-product HCl in continuity method production processes of chloroacetic acid | |
| CN105540660A (en) | Production device for preparing ultra-pure zirconium oxychloride byproduct silicon tetrachloride by fluidizing chlorination of zircon sand | |
| CN101569817B (en) | Tail gas recycling method in trichlorosilane production | |
| CN101293840A (en) | Technique for recycling triethylamine from hydrochloric acid triethylamine water solution | |
| CN100361891C (en) | Method of removing and reclaiming free chlorine in hydrochloric acid of chlorized by-product | |
| CN105502491A (en) | Method for preparing ultrapure zirconium oxychloride and byproduct silicon tetrachloride through zircon sand boiling chlorination | |
| CN106242961A (en) | Production of chloroacetic acid equipment | |
| CN208054910U (en) | The processing system of by-product HCl in continuity method production processes of chloroacetic acid | |
| WO2019114739A1 (en) | Production process for chlorinated paraffin | |
| US20110233045A1 (en) | Method of purifying hydrochloric acid | |
| CN110127615A (en) | Mannheim proeess produces the online purification process of hydrochloric acid in Process of Potassium Sulfate | |
| CN105480948B (en) | A kind of aliphatic acid or fat acyl chloride chlorination production byproduct in process object hydrogen chloride circulation utilization method and system | |
| JP2009209059A (en) | Method for producing acetone from bio-ethanol | |
| CN215627706U (en) | Device for co-producing pentafluoroethane from tetrafluoroethylene | |
| CN218392293U (en) | System for preparing trichloroethylene and tetrachloroethylene by azeotropic separation | |
| CN1962064A (en) | Method for processing waste catalyst in production of pentafluoro ethane | |
| CN106044710A (en) | Method for purifying electron-grade hydrogen chloride | |
| CN105272839A (en) | Synthesis method of diphenyl ketone | |
| CN1752065A (en) | Green chemical technology for producing chloracetyl chloride | |
| CN109651072B (en) | Method for preparing chloroethane from hydrochloric acid containing sulfur dioxide | |
| CN208482225U (en) | A kind of hydrogen chloride purification and recovery system | |
| CN114477094B (en) | Deep desorption process for hydrochloric acid | |
| CN101367708B (en) | Preparation of chloro-cyclohexane under nitrogen protection | |
| CN110862296A (en) | Method for separating reaction product in chloromethane production process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |