CN115228233A - Method for recovering dichloromethane waste gas - Google Patents
Method for recovering dichloromethane waste gas Download PDFInfo
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- CN115228233A CN115228233A CN202210839715.0A CN202210839715A CN115228233A CN 115228233 A CN115228233 A CN 115228233A CN 202210839715 A CN202210839715 A CN 202210839715A CN 115228233 A CN115228233 A CN 115228233A
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- condensation
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- waste gas
- dichloromethane
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- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 title claims abstract description 275
- 239000002912 waste gas Substances 0.000 title claims abstract description 77
- 238000000034 method Methods 0.000 title claims abstract description 28
- 238000009833 condensation Methods 0.000 claims abstract description 123
- 230000005494 condensation Effects 0.000 claims abstract description 123
- 238000011084 recovery Methods 0.000 claims abstract description 35
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 20
- 239000003507 refrigerant Substances 0.000 claims description 20
- 239000002826 coolant Substances 0.000 claims description 19
- 239000000243 solution Substances 0.000 claims description 16
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 12
- 239000007789 gas Substances 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 11
- 229910052757 nitrogen Inorganic materials 0.000 claims description 10
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 8
- 239000007864 aqueous solution Substances 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 4
- 239000003344 environmental pollutant Substances 0.000 abstract description 6
- 231100000719 pollutant Toxicity 0.000 abstract description 6
- IDGUHHHQCWSQLU-UHFFFAOYSA-N ethanol;hydrate Chemical compound O.CCO IDGUHHHQCWSQLU-UHFFFAOYSA-N 0.000 description 12
- 239000002808 molecular sieve Substances 0.000 description 8
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 8
- 230000000052 comparative effect Effects 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000013526 supercooled liquid Substances 0.000 description 2
- LVGUZGTVOIAKKC-UHFFFAOYSA-N 1,1,1,2-tetrafluoroethane Chemical compound FCC(F)(F)F LVGUZGTVOIAKKC-UHFFFAOYSA-N 0.000 description 1
- WGZYQOSEVSXDNI-UHFFFAOYSA-N 1,1,2-trifluoroethane Chemical compound FCC(F)F WGZYQOSEVSXDNI-UHFFFAOYSA-N 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- GTLACDSXYULKMZ-UHFFFAOYSA-N pentafluoroethane Chemical compound FC(F)C(F)(F)F GTLACDSXYULKMZ-UHFFFAOYSA-N 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Classifications
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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
- B01D53/002—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 condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0036—Multiple-effect condensation; Fractional condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/206—Organic halogen compounds
- B01D2257/2064—Chlorine
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a dichloromethane waste gas recovery method, which comprises the following steps: (1) Carrying out primary condensation on dichloromethane waste gas by a primary condensation system, wherein the temperature of the primary condensation is 1-5 ℃; (2) Carrying out secondary condensation on the dichloromethane waste gas after the primary condensation through a secondary condensation system, wherein the temperature of the secondary condensation is-40 to-45 ℃; (3) And (3) carrying out third-stage condensation on the dichloromethane waste gas subjected to the second-stage condensation through a third-stage condensation system, wherein the temperature of the third-stage condensation is-85 to-90 ℃. The dichloromethane waste gas recovery method can shorten the process time and avoid the generation of secondary pollutants under the condition of not influencing the dichloromethane recovery efficiency.
Description
Technical Field
The invention belongs to the technical field of waste gas recovery, and particularly relates to a dichloromethane waste gas recovery method.
Background
Dichloromethane (DCM) is a non-flammable low boiling solvent and is often used in industrial processes. Because the waste gas has low boiling point and is easy to volatilize in industrial production, the waste gas of industrial part contains dichloromethane, and the direct discharge of the waste gas of dichloromethane causes great pollution to the atmosphere, damages the body of operators and influences the environment of surrounding living residents, so the waste gas of dichloromethane needs to be recycled.
The existing dichloromethane waste gas recovery method mainly comprises the following steps: two-stage condensation, molecular sieve adsorption, water vapor desorption and condensation regeneration, wherein the molecular sieve is high in adsorption saturation and desorption times, so that the replacement frequency of the molecular sieve is high, and the whole recovery step is complex and time-consuming; meanwhile, a large amount of dangerous molecular sieve waste is generated, so that more secondary pollutants are generated in the conventional method for recovering the dichloromethane waste gas. Therefore, how to shorten the process time without affecting the recovery efficiency of dichloromethane and avoid the generation of secondary pollutants is a problem generally concerned by people at present, however, no corresponding process exists at present, and no relevant report is found.
Therefore, a method for recovering dichloromethane waste gas is needed to solve the problems of the prior art.
Disclosure of Invention
The invention aims to provide a dichloromethane waste gas recovery method, which can shorten the process time and avoid the generation of secondary pollutants under the condition of not influencing the dichloromethane recovery efficiency.
In order to achieve the above object, the present invention provides a dichloromethane waste gas recovery method, comprising the steps of:
(1) Carrying out primary condensation on dichloromethane waste gas by a primary condensation system, wherein the temperature of the primary condensation is 1-5 ℃;
(2) Carrying out secondary condensation on the dichloromethane waste gas after the primary condensation through a secondary condensation system, wherein the temperature of the secondary condensation is-40 to-45 ℃;
(3) And (3) carrying out third-stage condensation on the dichloromethane waste gas subjected to the second-stage condensation through a third-stage condensation system, wherein the temperature of the third-stage condensation is-85 to-90 ℃.
Compared with the prior art, the dichloromethane waste gas recovery method adopts the first-stage condensation, the second-stage condensation and the third-stage condensation, the temperature of the first-stage condensation is 1-5 ℃ to carry out low-temperature treatment on the dichloromethane waste gas, the temperature of the second-stage condensation is-40 to-45 ℃ to carry out normal cooling treatment on the dichloromethane waste gas, and the temperature of the third-stage condensation is-85 to-90 ℃ to carry out deep cooling treatment on the dichloromethane waste gas, so that the dichloromethane waste gas recovery method only adopts the third-stage condensation to treat the dichloromethane waste gas, the recovery efficiency can exceed 99 percent, and the adsorption of a molecular sieve is not needed, thereby obviously shortening the process time, simultaneously avoiding a large amount of dangerous molecular sieve wastes and solving the problem of generation of secondary pollutants.
Preferably, the temperature of the first stage condensation of the present invention is 3 ℃.
Preferably, the temperature of the second stage condensation of the present invention is-40 ℃.
Preferably, the temperature of the third stage of condensation of the present invention is-90 ℃. The mass of the dichloromethane is 500g/m 3 About, the molecular weight of the dichloromethane is 84.93, the specific heat is 0.992kj/kg, the latent heat of vaporization is 329.5kj/kg, the condensation point is-97 ℃, and the gaseous dichloromethane is basically converted into liquid at the temperature of-97 ℃, but the inventor finds that the recovery efficiency is highest when the temperature of the first stage of condensation is 3 ℃, the temperature of the second stage of condensation is-40 ℃ and the temperature of the third stage of condensation is-90 ℃ in the invention creation process, and simultaneously the energy consumption is relatively lowest.
Preferably, the main components of the dichloromethane waste gas of the invention are dichloromethane and air, and the concentration of the dichloromethane in the dichloromethane waste gas is 450-500 g/m 3 Therefore, the methylene dichloride waste gas recovery method of the invention is suitable for the recovery of high-concentration methylene dichloride waste gas.
Preferably, the first stage condensation system, the second stage condensation system and the third stage condensation system of the invention have different cooling media.
Preferably, the cooling medium of the first stage condensation system and the second stage condensation system of the present invention each comprise a refrigerant and a coolant, the refrigerant comprises at least one of R404A, R23, R125 and R14, and the coolant comprises at least one of a heat transfer oil, an aqueous solution of ethylene glycol and an aqueous solution of ethanol. Wherein R404A is formed by mixing HFC125, HFC-134A and HFC-143; r23 is CHF 3 (ii) a R125 is CF 2 CF 3 (ii) a R14 is CF 4 。
Preferably, the cooling medium of the third stage condensation system of the present invention is a third stage refrigerant and a third stage secondary refrigerant, the third stage refrigerant is liquid nitrogen, and the third stage secondary refrigerant comprises at least one of heat transfer oil, an aqueous solution of ethylene glycol and an aqueous solution of ethanol.
Drawings
FIG. 1 is a schematic diagram of the first stage condensing system of the present invention.
Fig. 2 is a schematic diagram of the third stage condensing system of the present invention.
Detailed Description
To better illustrate the objects, technical solutions and advantages of the present invention, the present invention will be further described with reference to specific examples. It should be noted that the following implementation of the method is to further explain the invention, and should not be construed as a limitation of the invention.
The working principle of the first stage condensing system and the second stage condensing system of the present invention is the same, referring to fig. 1, the working principle of the first stage condensing system 100 of the present invention is described as follows:
first stage condensing system 100: the system comprises a compressor 11, a condenser 12, an expansion valve 13, an evaporator 14 and an exhaust gas cold box catcher 15, wherein the compressor 11, the condenser 12, the expansion valve 13 and the evaporator 14 are sequentially connected through a first pipeline 16, and a refrigerant circulates in the first pipeline 16 under the connection relationship; the evaporator 14 and the exhaust gas cold box catcher 15 are also connected by a second pipeline 17, a circulating pump 18 is arranged on the second pipeline 17, and the inside of the second pipeline 17 under the connection relationship is a secondary refrigerant circulation. When the first-stage condensing system 100 works, high-temperature and high-pressure refrigerant gas discharged by the compressor 11 enters the condenser 12 to be condensed into high-pressure supercooled liquid, the high-pressure supercooled liquid is throttled by the expansion valve 13 and is reduced in pressure to become low-temperature and low-pressure liquid phase, the liquid phase enters the evaporator 14, the refrigerant absorbs cold energy of secondary refrigerant passing through the evaporator 14 in the liquid phase to be gasified, the refrigerant is fully gasified and then is sucked into a compression chamber by the compressor 11 to enter the next cycle, and the secondary refrigerant is conveyed to the waste gas cold box catcher 15 through the large-flow circulating pump 18 to exchange heat with waste gas.
Referring to fig. 2, the operation of the third stage condensing system 200 of the present invention is illustrated as follows:
third stage condensing system 200: the system comprises a liquid nitrogen tank 21, a valve box 22, a heat exchanger 23, a three-stage circulating pump 26 and a three-stage waste gas cold box trap 24, wherein the liquid nitrogen tank 21 is connected with an input end 221 of the valve box 22, a low-temperature electromagnetic valve (not shown in the figure) is arranged in the valve box 22, an output end 222 of the valve box 22 is connected with the heat exchanger 23, the heat exchanger 23 and the three-stage waste gas cold box trap 24 are also connected through a third pipeline 25, the third pipeline 25 is provided with the three-stage circulating pump 26, and three-stage secondary refrigerant circulates in the third pipeline 25 under the connection relation. When the third-stage condensing system 200 works, liquid nitrogen in the liquid nitrogen tank 21 enters the heat exchanger 23 through the low-temperature electromagnetic valve, the third-stage secondary refrigerant exchanges heat in the heat exchanger to obtain stable temperature, and the third-stage secondary refrigerant is conveyed to the third-stage waste gas cold box catcher 24 through the large-flow third-stage circulating pump 26 to exchange heat with waste gas.
Example 1
This example 1 provides a dichloromethane waste gas recovery method, including the steps:
(1) The temperature is 39 ℃ and the concentration is 500g/m 3 The dichloromethane waste gas is subjected to first-stage condensation by a first-stage condensation system to obtain the dichloromethane waste gas with the concentration of 472.654g/m 3 Dichloromethane waste gas, wherein the temperature of the first-stage condensation is 3 ℃, and the cooling medium of the first-stage condensation system comprises R404A and ethanol water solution;
(2) The dichloromethane waste gas after the first stage condensation is subjected to second stage condensation by a second stage condensation system to obtain the dichloromethane with the concentration of 84.530g/m 3 Dichloromethane waste gas, wherein the temperature of the secondary condensation is-40 ℃, and the cooling medium of the secondary condensation system comprises R125 and ethanol water;
(3) The dichloromethane waste gas after the second stage condensation is subjected to third stage condensation by a third stage condensation system to obtain the dichloromethane with the concentration of 0.762g/m 3 The recovery efficiency of the dichloromethane waste gas is 99.85 percent, wherein the temperature of the third-stage condensation is-90 ℃, and the cooling medium of the third-stage condensation system is liquid nitrogen and ethanol water solution.
Example 2
The embodiment 2 provides a dichloromethane waste gas recovery method, which comprises the following steps:
(1) The temperature is 39 ℃ and the concentration is 500g/m 3 The dichloromethane waste gas is subjected to first-stage condensation by a first-stage condensation system to obtain the dichloromethane waste gas with the concentration of 489.925g/m 3 Dichloromethane waste gas, wherein the temperature of the first-stage condensation is 5 ℃, and the cooling medium of the first-stage condensation system comprises R404A and ethanol water solution;
(2) The dichloromethane waste gas after the first stage condensation is subjected to second stage condensation by a second stage condensation system to obtain the dichloromethane waste gas with the concentration of 72.212g/m 3 Dichloromethane waste gas, wherein the temperature of the secondary condensation is-43 ℃, and the cooling medium of the secondary condensation system comprises R125 and ethanol water solution;
(3) The dichloromethane waste gas after the second stage condensation is subjected to third stage condensation by a third stage condensation system to obtain the dichloromethane waste gas with the concentration of 1.135g/m 3 The recovery efficiency of the dichloromethane waste gas is 99.77 percent, wherein the temperature of the third stage condensation is-88 ℃, and the cooling medium of the third stage condensation system is liquid nitrogen and ethanol water solution.
Example 3
This example 3 provides a dichloromethane off-gas recovery method, which includes the steps of:
(1) The temperature is 39 ℃ and the concentration is 500g/m 3 The dichloromethane waste gas is subjected to first-stage condensation by a first-stage condensation system to obtain the dichloromethane waste gas with the concentration of 467.871g/m 3 Dichloromethane waste gas, wherein the temperature of the first stage condensation is 1 ℃, and the cooling medium of the first stage condensation system comprises R404A and ethanol water;
(2) The dichloromethane waste gas after the first stage condensation is subjected to second stage condensation by a second stage condensation system to obtain the dichloromethane with the concentration of 69.009g/m 3 Dichloromethane waste gas, wherein the temperature of the secondary condensation is-45 ℃, and the cooling medium of the secondary condensation system comprises R125 and ethanol water solution;
(3) The dichloromethane waste gas after the second stage condensation is subjected to third stage condensation by a third stage condensation system to obtain the dichloromethane with the concentration of 1.438g/m 3 The recovery efficiency of the dichloromethane waste gas is 99.71 percent, wherein the temperature of the third stage condensation is-85 ℃, and the cooling medium of the third stage condensation system is liquid nitrogen and ethanol water solution.
Comparative example 1
This comparative example 1 provides a methylene chloride off-gas recovery method comprising the steps of:
(1) The temperature is 39 ℃ and the concentration is 500g/m 3 The dichloromethane waste gas is subjected to first-stage condensation by a first-stage condensation system to obtain the dichloromethane waste gas with the concentration of 472.654g/m 3 Dichloromethane waste gas, wherein the temperature of the first-stage condensation is 3 ℃, and the cooling medium of the first-stage condensation system comprises R404A and ethanol water solution;
(2) The dichloromethane waste gas after the first stage condensation is subjected to second stage condensation by a second stage condensation system to obtain the concentration of 447.934g/m 3 Dichloromethane waste gas, wherein the temperature of the secondary condensation is-10 ℃, and the cooling medium of the secondary condensation system comprises R125 and ethanol water solution;
(3) The dichloromethane waste gas after the second stage condensation is subjected to third stage condensation by a third stage condensation system to obtain the dichloromethane waste gas with the concentration of 265.973g/m 3 The recovery efficiency of the dichloromethane waste gas is 46.81 percent, wherein the temperature of the third stage condensation is-20 ℃, and the cooling medium of the third stage condensation system is liquid nitrogen and ethanol water solution.
As can be seen from the above examples and comparative example 1, the recovery efficiency of dichloromethane of all examples is higher than that of comparative example 1, which shows that the recovery efficiency of dichloromethane waste gas is over 99% by only using the first stage condensation (1-5 ℃), the second stage condensation (-40 to-45 ℃) and the third stage condensation (-85 to-90 ℃) to treat dichloromethane waste gas, so that the recovery efficiency of dichloromethane waste gas of the invention is not affected by the adsorption of molecular sieve, which obviously shortens the process time, avoids a large amount of dangerous molecular sieve wastes and solves the problem of secondary pollutant generation.
Finally, it should be noted that the above embodiments are only used for illustrating the technical solutions of the present invention and not for limiting the protection scope of the present invention, and although the present invention is described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications or equivalent substitutions can be made on the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention.
Claims (8)
1. A dichloromethane waste gas recovery method is characterized by comprising the following steps:
(1) Carrying out primary condensation on dichloromethane waste gas by a primary condensation system, wherein the temperature of the primary condensation is 1-5 ℃;
(2) Carrying out secondary condensation on the dichloromethane waste gas after the primary condensation through a secondary condensation system, wherein the temperature of the secondary condensation is-40 to-45 ℃;
(3) And carrying out third-stage condensation on the dichloromethane waste gas subjected to the second-stage condensation through a third-stage condensation system, wherein the temperature of the third-stage condensation is-85 to-90 ℃.
2. The methylene dichloride off-gas recovery process of claim 1 wherein the temperature of the first stage condensation is 3 ℃.
3. The methylene dichloride off gas recovery process of claim 1 wherein the temperature of the second stage condensation is-40 ℃.
4. The methylene dichloride off-gas recovery process of claim 1 wherein the temperature of the third stage condensation is-90 ℃.
5. The method according to claim 1, wherein the concentration of dichloromethane in the dichloromethane off-gas is 450 to 500g/m 3 。
6. The methylene dichloride off-gas recovery process of claim 1 wherein the first stage condensation system, the second stage condensation system, the third stage condensation system differ in cooling medium.
7. The dichloromethane exhaust gas recovery method according to claim 6, wherein the cooling media of the first stage condensation system and the second stage condensation system comprise refrigerants and secondary refrigerants, the refrigerants comprise at least one of R404A, R23, R125 and R14, and the secondary refrigerants comprise at least one of heat transfer oil, ethylene glycol aqueous solution and ethanol aqueous solution.
8. The methylene dichloride exhaust gas recovery method according to claim 6, wherein the cooling medium of the third stage condensation system is liquid nitrogen and a third stage coolant comprising at least one of a heat transfer oil, an aqueous ethylene glycol solution and an aqueous ethanol solution.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202210839715.0A CN115228233A (en) | 2022-07-15 | 2022-07-15 | Method for recovering dichloromethane waste gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210839715.0A CN115228233A (en) | 2022-07-15 | 2022-07-15 | Method for recovering dichloromethane waste gas |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4265837A (en) * | 1978-05-02 | 1981-05-05 | Hoechst Aktiengesellschaft | Production of 1,2-dichloroethane |
| CN103203157A (en) * | 2013-03-20 | 2013-07-17 | 杭州中环环保工程有限公司 | Dichloromethane waste gas treating method and system thereof |
| CN106390672A (en) * | 2016-11-15 | 2017-02-15 | 刘代学 | Method of recycling dichloromethane in waste gas |
| CN108339370A (en) * | 2018-01-09 | 2018-07-31 | 浙江东天虹环保工程有限公司 | A kind of high concentration dichloromethane waste gas recovery reuse method and system |
| CN212236622U (en) * | 2019-12-12 | 2020-12-29 | 广东立国制药有限公司 | Dichloromethane tail gas recovery system |
| CN215842402U (en) * | 2021-09-14 | 2022-02-18 | 河北思普森环保科技有限公司 | Dichloromethane recycling and purifying device |
-
2022
- 2022-07-15 CN CN202210839715.0A patent/CN115228233A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4265837A (en) * | 1978-05-02 | 1981-05-05 | Hoechst Aktiengesellschaft | Production of 1,2-dichloroethane |
| CN103203157A (en) * | 2013-03-20 | 2013-07-17 | 杭州中环环保工程有限公司 | Dichloromethane waste gas treating method and system thereof |
| CN106390672A (en) * | 2016-11-15 | 2017-02-15 | 刘代学 | Method of recycling dichloromethane in waste gas |
| CN108339370A (en) * | 2018-01-09 | 2018-07-31 | 浙江东天虹环保工程有限公司 | A kind of high concentration dichloromethane waste gas recovery reuse method and system |
| CN212236622U (en) * | 2019-12-12 | 2020-12-29 | 广东立国制药有限公司 | Dichloromethane tail gas recovery system |
| CN215842402U (en) * | 2021-09-14 | 2022-02-18 | 河北思普森环保科技有限公司 | Dichloromethane recycling and purifying device |
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