CN108939794A - A kind of recovery method of trichloroethane gas - Google Patents
A kind of recovery method of trichloroethane gas Download PDFInfo
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- CN108939794A CN108939794A CN201810778496.3A CN201810778496A CN108939794A CN 108939794 A CN108939794 A CN 108939794A CN 201810778496 A CN201810778496 A CN 201810778496A CN 108939794 A CN108939794 A CN 108939794A
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- absorber
- trichloroethanes
- recovery method
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- trichloroethane
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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
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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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0454—Controlling adsorption
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C19/00—Acyclic saturated compounds containing halogen atoms
- C07C19/01—Acyclic saturated compounds containing halogen atoms containing chlorine
- C07C19/043—Chloroethanes
- C07C19/05—Trichloroethanes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/20—Organic adsorbents
- B01D2253/202—Polymeric adsorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/402—Further details for adsorption processes and devices using two beds
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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)
- Organic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention provides a kind of recovery method of trichloroethane gas, and exhaust gas will be obtained containing trichloroethanes and carries out B-grade condensation, adsorption and desorption and three-level condensation, has high-recovery, cheap operating cost, with good economic efficiency and social benefit.
Description
Technical field
The invention belongs to waste gas recovery technologies, and in particular to a kind of recovery method of trichloroethane gas.
Background technique
Sweetener manufacturing enterprise uses a large amount of trichloroethanes as solvent, generates largely containing the exhaust gas of trichloroethanes,
Existing recovery method is recycled using multi-stage condensing mode, and the rate of recovery is up to 98% or more, remaining micro on-condensible gas row
Out；But bigger due to applying total amount daily, the on-condensible gas for accumulating discharge also has certain quantity, to plant area and surrounding enviroment
Still certain influence can be generated, in the environment of at present to environmentally friendly unprecedented attention, existing waste gas recovery mode is still inadequate
It is perfect.
The processing method of organic exhaust gas is various, and feature is different, there are commonly condensation method, absorption process, combustion method, absorption method,
Embrane method etc..
(1) combustion method includes high-temp combustion and catalysis burning, the former needs additional fuel to burn, therefore, when using the method
Consider to recycle thermal energy, while not exclusively generating the secondary pollutions substances such as dioxin, phosgene, Bu Nengyong in order to avoid reacting
To handle chlorohydrocarbon.Low energy consumption for catalysis burning, but chlorohydrocarbon is easy to make catalyst poisoning.Therefore this project is not suitable for using burning
Method；
(2) absorption process is absorbed in absorption tower using absorbent appropriate (such as diesel oil, kerosene, water medium),
It is absorbed into the separation that solvent and absorbing liquid are carried out after a certain concentration, solvent recovery, absorbing liquid is reused or otherwise processed, uses
The key of this method is the selection of absorbent.Since the separation of solvent and absorbent is more difficult, application is received
Certain limitation；
(3) absorption method absorption method processing organic exhaust gas technique has been widely used, the basic principle is that utilizing porous adsorbent
Porous structure absorption organic exhaust gas in VOCs, and this adsorption process is mostly physical absorption, after adsorbent adsorption saturation,
Reusable heat air or vapor are desorbed, and regenerated adsorbent may be reused.Commercialized adsorbent mainly includes
Active carbon, activated carbon fiber, mesopore molecular sieve, resin sorbent etc..It is middle low concentration that absorption method, which is most suitable for concentration for the treatment of,
VOCs has good solvent recovery effect；
(4) condensation method is mainly handled high temperature organic exhaust gas steam using cold medium, can effective recycling design.Processing
The quality of effect is related with the temperature of refrigerant, and treatment effeciency is relatively low compared with other methods, is applicable in the processing of high-concentration waste gas.It is cold
Solidifying technique is mainly used for the recycling of higher boiling or high concentration VOCs, will not generally be used alone, and before being used in other techniques
Processing stage.
Therefore, there is an urgent need to provide a kind of comprehensive recovering process with the higher rate of recovery to carry out trichloroethane gas
Recycling.
Summary of the invention
It is an object of the invention to overcome the recovery method rate of recovery of trichloroethane gas in the prior art not ideal enough, and
Provide a kind of recovery method of the cheap trichloroethane gas of ultrahigh-recovery-rate, operating cost.
The present invention provides a kind of recovery methods of trichloroethane gas, it is characterised in that includes the following steps:
(1) exhaust gas containing trichloroethanes of discharge is subjected to B-grade condensation；
(2) exhaust gas containing trichloroethanes after separating B-grade condensation is discharged into adsorbent equipment；
(3) adsorbent equipment includes absorber A and absorber B, and through operation after a period of time, absorber A saturation then switches
It is adsorbed to absorber B, absorber A is passed through water vapour and is desorbed；Absorber A replaces absorber B and works on after the completion of desorption,
Absorber B is desorbed, and is circuited sequentially；
(4) trichloroethanes desorbed and vapor are mixed aqueous vapor object to condense through three-level condenser, obtains trichloroethanes
With the mixture of water, trichloroethanes is obtained through static layering.
Preferably, the adsorbent material loaded in the adsorbent equipment be active carbon, mesopore molecular sieve, resin sorbent or
HEA adsorbent.
Preferably, first order condensation temperature is 0~35 DEG C in the step (1), and second level condensation temperature is 0~10 DEG C.
Preferably, first order condensation air pressure is 0.1~0.2MPa in the step (1)；The second level condense air pressure be 0.1~
0.2MPa。
Preferably, air pressure is 0.1~0.3MPa when vapor is desorbed in the step (3).
Preferably, absorber A is carried out with cooling blower and heat exchanger after the completion of absorber A desorption in the step (3)
Interior circulating cooling；Stopping when absorber A is cooled to set temperature
The beneficial effects of the present invention are: the recovery method of trichloroethane gas provided by the invention has high-recovery, low
Honest and clean operating cost, with good economic efficiency and social benefit.
Specific embodiment
Illustrate technical solution of the present invention below by way of specific embodiment, but the scope of the present invention is not limited thereto.
Embodiment 1
Trichloroethanes exhaust gas is through carrying out B-grade condensation, and wherein level-one condensation cycle coolant-temperature gage is 25 DEG C, B-grade condensation circulation
Coolant-temperature gage is 5 DEG C；The air quantity of the total discharge outlet of trichloroethanes is about 4900m after condensed in two stages3/ h, gas concentration 16g/m3
Practical discharge rate is about 1.88t/d, and emission equivalent is to discharge for 24 hours, and gas is saturated humidity, and temperature is room temperature；By main air blower
It is discharged after introducing absorber A；Through operation after a period of time, absorber A saturation then switches to absorber B absorption, absorber A
Steam is passed through to be desorbed.Interior circulating cooling is carried out to absorber A with cooling blower and heat exchanger after the completion of absorber A desorption.
Stopping when absorber A is cooled to set temperature, hereafter can be adsorbed again.A B absorber adsorption and desorption and cold in turn
But, whenever, there is an absorber to be in adsorbed state.Air pressure is 0.2MPa when vapor is desorbed.It is filled in absorber
The adsorbent of load is active carbon particle, and partial size is 100~200 mesh.
The steam being desorbed out condenses after heat exchanger, and condensed liquid obtains three chloroethenes after stratification into slot is layered
Alkane and condensed water, and store respectively.
The trichloroethanes desorbed and vapor are mixed aqueous vapor object to condense through three-level condenser, obtain trichloroethanes and water
Mixture, obtain trichloroethanes through static layering.It is computed, trichloroethanes overall recovery is 99.5%.Using the prior art
Multi-stage condensing scheme, trichloroethanes overall recovery be 98%.
A certain amount of waste liquid can be generated in device operational process, waste liquid amount is close with steam consumption, can be emitted into nearby
Sewage disposal system.
Embodiment 2
Trichloroethanes exhaust gas is through carrying out B-grade condensation, and wherein level-one condensation cycle coolant-temperature gage is 20 DEG C, B-grade condensation circulation
Coolant-temperature gage is 5 DEG C；The air quantity of the total discharge outlet of trichloroethanes is about 4900m after condensed in two stages3/ h, gas concentration 16g/m3
Practical discharge rate is about 1.88t/d, and emission equivalent is to discharge for 24 hours, and gas is saturated humidity, and temperature is room temperature；By main air blower
It is discharged after introducing absorber A；Through operation after a period of time, absorber A saturation then switches to absorber B absorption, absorber A
Steam is passed through to be desorbed.Interior circulating cooling is carried out to absorber A with cooling blower and heat exchanger after the completion of absorber A desorption.
Stopping when absorber A is cooled to set temperature, hereafter can be adsorbed again.A B absorber adsorption and desorption and cold in turn
But, whenever, there is an absorber to be in adsorbed state.Air pressure is 0.2MPa when vapor is desorbed.It is filled in absorber
The adsorbent of load is HEA adsorbent.The HEA adsorbent is produced by Jiangsu Ke Yue Environmental Protection Technology Co., Ltd.
The trichloroethanes desorbed and vapor are mixed aqueous vapor object to condense through three-level condenser, obtain trichloroethanes and water
Mixture, obtain trichloroethanes through static layering.
The steam being desorbed out condenses after heat exchanger, and condensed liquid obtains three chloroethenes after stratification into slot is layered
Alkane and condensed water, and store respectively.It is computed, trichloroethanes overall recovery is 99.8%.
A certain amount of waste liquid can be generated in device operational process, waste liquid amount is close with steam consumption, can be emitted into nearby
Sewage disposal system.
Operating cost and income are listed in Table 1 below:
Table 1
Above-mentioned income is the result compared with using the multi-stage condensing scheme of the prior art.
The comparative situation of acticarbon used in Examples 1 and 2 and HEA adsorbent material is listed in table 2.
Table 2
Taking the above-mentioned ideal embodiment according to the present invention as inspiration, through the above description, relevant staff is complete
Various changes and amendments can be carried out without departing from the scope of the technological thought of the present invention' entirely.The technology of this invention
Property range is not limited to the contents of the specification, it is necessary to which the technical scope thereof is determined according to the scope of the claim.
Claims (6)
1. a kind of recovery method of trichloroethane gas, it is characterised in that include the following steps:
(1) exhaust gas containing trichloroethanes of discharge is subjected to B-grade condensation；
(2) exhaust gas containing trichloroethanes after separating B-grade condensation is discharged into adsorbent equipment；
(3) adsorbent equipment includes absorber A and absorber B, and through operation after a period of time, absorber A saturation then switches to suction
Adnexa B absorption, absorber A are passed through water vapour and are desorbed；Absorber A replaces absorber B and works on after the completion of desorption, adsorbs
Device B is desorbed, and is circuited sequentially；
(4) trichloroethanes desorbed and vapor are mixed aqueous vapor object to condense through three-level condenser, obtains trichloroethanes and water
Mixture, obtain trichloroethanes through static layering.
2. the recovery method of trichloroethane gas as described in claim 1, which is characterized in that loaded in the adsorbent equipment
Adsorbent material is active carbon, mesopore molecular sieve, resin sorbent or HEA adsorbent.
3. the recovery method of trichloroethane gas as described in claim 1, which is characterized in that the first order in the step (1)
Condensation temperature is 0~35 DEG C, and second level condensation temperature is 0~10 DEG C.
4. the recovery method of trichloroethane gas as described in claim 1, which is characterized in that the first order in the step (1)
Condensation air pressure is 0.1 ~ 0.2MPa；It is 0.1 ~ 0.2MPa that the second level, which condenses air pressure,.
5. the recovery method of trichloroethane gas as described in claim 1, which is characterized in that vapor in the step (3)
Air pressure is 0.1 ~ 0.3MPa when desorption.
6. such as the recovery method of the described in any item trichloroethane gas of claim 1 ~ 5, which is characterized in that the step (3)
Interior circulating cooling is carried out to absorber A with cooling blower and heat exchanger after the completion of middle absorber A desorption；Until absorber A is cooling
Stop when to set temperature.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810778496.3A CN108939794A (en) | 2018-07-16 | 2018-07-16 | A kind of recovery method of trichloroethane gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810778496.3A CN108939794A (en) | 2018-07-16 | 2018-07-16 | A kind of recovery method of trichloroethane gas |
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| CN108939794A true CN108939794A (en) | 2018-12-07 |
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| CN201810778496.3A Pending CN108939794A (en) | 2018-07-16 | 2018-07-16 | A kind of recovery method of trichloroethane gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109503314A (en) * | 2018-12-10 | 2019-03-22 | 安徽金禾实业股份有限公司 | A kind of Sucralose produces the recovery method of trichloroethanes in tail gas |
| CN116272232A (en) * | 2023-02-22 | 2023-06-23 | 苏州博瑞达高分子材料有限公司 | Condensation recovery device and method for brominated epoxy resin |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106390672A (en) * | 2016-11-15 | 2017-02-15 | 刘代学 | Method of recycling dichloromethane in waste gas |
| CN107008103A (en) * | 2017-05-05 | 2017-08-04 | 上海化工研究院有限公司 | A kind of method of volatile chlorinated hydrocarbon in physical absorption abjection gas phase |
-
2018
- 2018-07-16 CN CN201810778496.3A patent/CN108939794A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106390672A (en) * | 2016-11-15 | 2017-02-15 | 刘代学 | Method of recycling dichloromethane in waste gas |
| CN107008103A (en) * | 2017-05-05 | 2017-08-04 | 上海化工研究院有限公司 | A kind of method of volatile chlorinated hydrocarbon in physical absorption abjection gas phase |
Non-Patent Citations (1)
| Title |
|---|
| 赵英杰等: "《VOCs概况及案例研究》", 28 February 2018, 科学技术文献出版社 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109503314A (en) * | 2018-12-10 | 2019-03-22 | 安徽金禾实业股份有限公司 | A kind of Sucralose produces the recovery method of trichloroethanes in tail gas |
| CN116272232A (en) * | 2023-02-22 | 2023-06-23 | 苏州博瑞达高分子材料有限公司 | Condensation recovery device and method for brominated epoxy resin |
| CN116272232B (en) * | 2023-02-22 | 2024-04-05 | 苏州博瑞达高分子材料有限公司 | Condensation recovery device and method for brominated epoxy resin |
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