CN104324598A - Method for purifying tail gas produced in synthesis of mercury catalyst - Google Patents
Method for purifying tail gas produced in synthesis of mercury catalyst Download PDFInfo
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- CN104324598A CN104324598A CN201410617981.4A CN201410617981A CN104324598A CN 104324598 A CN104324598 A CN 104324598A CN 201410617981 A CN201410617981 A CN 201410617981A CN 104324598 A CN104324598 A CN 104324598A
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Abstract
The invention discloses a method for purifying tail gas produced in synthesis of a mercury catalyst. The method comprises the following steps: sending the tail gas discharged by a dehumidification device used in the production of the mercuric chloride catalyst into a dust collection device for dust collection operation; then, carrying out heat exchange on the tail gas entering a heat exchanger for recovering waste heat, and cooling the tail gas to 40-60 DEG C; after the waste heat of the tail gas is recovered, sending the tail gas to the lower part of a packed tower, enabling the tail gas to enter the packed tower from the lower part of the packed tower, and washing the tail gas, wherein a mixed solution of 4wt%-12wt% of BaCl2 solution, 10wt%-20wt% of Ca(OH)2 solution and 10wt%-20wt% of ammonia water are taken as a washing solution, the mass ratio of the BaCl2 solution to the Ca(OH)2 solution to the ammonia water is (4-6) to (7-10) to (3-4), the tail gas in the tower are washed in a spraying manner by the washing solution sprayed by nozzles arranged on the top and in the middle of the packed tower, and countercurrent washing is adopted in the packed tower. The washing solution is recycled, and a new washing solution is supplemented when the concentration of the washing solution is reduced; an adsorption device is arranged at a tail gas outlet on the top of the packed tower, the tail gas is discharged after passing through the adsorption device, and the adsorption device is internally provided with an adsorbent; the adsorbent is a compound adsorbent and comprises 20wt%-60wt% of activated carbon, 20wt%-40wt% of ZSM-11 and 20wt%-30wt% of Y type zeolite. After the method is adopted, the tail gas can be discharged after reaching the standard, the content of mercury in the tail gas is very low, and the emission standard in China is met.
Description
Technical field
The present invention relates to the method for the tail gas that a kind of purification produces in synthesis mercury catalyst.
Background technology
Be exposed in high-load mercury and can produce serious nerve and development impact to the mankind.The concentration of air-borne mercury is usually very low and impact is very micro-, but once mercury enters in water, it can accumulate and produce harm to the people of this mercury-contaminated fish edible in fish.The catalyst of mercuric chleride catalyst raw material " calcium carbide one acetylene " method synthesizing chloroethylene monomer (VCM) based on Coal Chemical Industry, is widely used in PVC Industry acetylene method PVC.In mercuric chleride catalyst production process, main containing 10-2000mg/Nm in its tail gas produced
3mercury chloride and 1-100mg/Nm
3hydrochloric acid (HCl); When producing regeneration mercuric chleride catalyst, also containing 1-50mg/Nm in its tail gas
3chlorine; Exhaust temperature is 90-105 DEG C.For these three kinds of noxious pollutants in tail gas, could discharge after environmental requirement has to pass through purified treatment.At present, the method of conventional process tail gas mainly contains two kinds: 1. active carbon adsorption, this process is carried out in a corrosion-resistant active carbon purifying processor, when tail gas is by this purification processing facility, mercury chloride is wherein tightly held by activated carbon, hydrochloric acid is adsorbed with the form of hydrochloric acid solution by active carbon, chlorine by active carbon with hypochlorous acid and hydrochloric acid (because of in tail gas containing a certain amount of water vapour, Cl
2with H
2o effect generate HClO and HCl) form adsorbed, in tail gas, waste heat does not reclaim.The shortcoming of the method is: the tail gas after process is almost difficult to qualified discharge, and active carbon is changed frequent, and meanwhile, using waste heat from tail gas is wasted.2., in alkali lye (NaOH solution) and absorption process, this process is that tail gas is fully contacted with NaOH solution, the HgCl in tail gas
2, HCl, Cl
2generate HgO, NaCl, NaClO with NaOH reactant aqueous solution, realize removing noxious pollutant in tail gas.Generally, the method is also not easy the tail gas after enabling purified treatment and realizes qualified discharge, mercury content particularly in tail gas, simultaneously, the solid waste that decontamination process produces, production mercuric chleride catalyst can not be directly used in, as mercurous refuse process, the hidden danger of secondary pollution can only be there is; Using waste heat from tail gas is not also recycled, causes energy dissipation.
Summary of the invention
The object of the invention is to the method proposing the tail gas that a kind of purification produces in synthesis mercury catalyst.
For reaching this object, the present invention by the following technical solutions:
The method of the tail gas that a kind of purification produces in synthesis mercury catalyst, comprise the following steps: that the tail gas ejected in dehydrating unit in mercuric chleride catalyst production is sent into dust arrester and carried out dust removal operation, enter heat exchanger subsequently and carry out heat exchange with recovery waste heat, make tail gas be cooled to 40-60 DEG C; Tail gas through recovery waste heat sends into packed tower bottom, enters in tower wash from packed tower bottom, adopts the BaCl of 4-12wt%
2the Ca (OH) of solution, 10-20wt%
2the mixed liquor of solution and 10-20wt% ammoniacal liquor as cleaning solution, BaCl
2solution, Ca (OH)
2the mass ratio of solution and ammoniacal liquor is 4-6:7-10:3-4, and the nozzle of cleaning solution in the middle part of filler tower top and tower carries out spray washing to tower inner exhaust gas respectively, is countercurrent washing in packed tower; Cleaning solution recycles, fresh wash liquid is supplemented after cleaning solution concentration reduces, at packed tower top, offgas outlet arranges adsorbent equipment, tail gas is by emptying after adsorbent equipment, adsorbent is provided with in adsorbent equipment, adsorbent is compound adsorbent, and it consists of the active carbon of 20-60wt%, the y-type zeolite of ZSM-11 and 20-30wt% of 20-40wt%.
The method can tail gas qualified discharge, and in tail gas, mercury content is extremely low, meets discharging standards.
Detailed description of the invention
Embodiment 1
The tail gas ejected in dehydrating unit in mercuric chleride catalyst production is sent into dust arrester and is carried out dust removal operation, enters heat exchanger subsequently and carries out heat exchange with recovery waste heat, make tail gas be cooled to 40-60 DEG C; Tail gas through recovery waste heat sends into packed tower bottom, enters in tower wash from packed tower bottom, adopts the BaCl of 4-12wt%
2the Ca (OH) of solution, 10-20wt%
2the mixed liquor of solution and 10-20wt% ammoniacal liquor as cleaning solution, BaCl
2solution, Ca (OH)
2the mass ratio of solution and ammoniacal liquor is 6:9:4, and the nozzle of cleaning solution in the middle part of filler tower top and tower carries out spray washing to tower inner exhaust gas respectively, is countercurrent washing in packed tower; Cleaning solution recycles, fresh wash liquid is supplemented after cleaning solution concentration reduces, at packed tower top, offgas outlet arranges adsorbent equipment, tail gas is by emptying after adsorbent equipment, adsorbent is provided with in adsorbent equipment, adsorbent is compound adsorbent, and it consists of the active carbon of 20-60wt%, the y-type zeolite of ZSM-11 and 20-30wt% of 20-40wt%.
Embodiment 2
The tail gas ejected in dehydrating unit in mercuric chleride catalyst production is sent into dust arrester and is carried out dust removal operation, enters heat exchanger subsequently and carries out heat exchange with recovery waste heat, make tail gas be cooled to 40-60 DEG C; Tail gas through recovery waste heat sends into packed tower bottom, enters in tower wash from packed tower bottom, adopts the BaCl of 4-12wt%
2the Ca (OH) of solution, 10-20wt%
2the mixed liquor of solution and 10-20wt% ammoniacal liquor as cleaning solution, BaCl
2solution, Ca (OH)
2the mass ratio of solution and ammoniacal liquor is 5:10:3, and the nozzle of cleaning solution in the middle part of filler tower top and tower carries out spray washing to tower inner exhaust gas respectively, is countercurrent washing in packed tower; Cleaning solution recycles, fresh wash liquid is supplemented after cleaning solution concentration reduces, at packed tower top, offgas outlet arranges adsorbent equipment, tail gas is by emptying after adsorbent equipment, adsorbent is provided with in adsorbent equipment, adsorbent is compound adsorbent, and it consists of the active carbon of 20-60wt%, the y-type zeolite of ZSM-11 and 20-30wt% of 20-40wt%.
Embodiment 3
The tail gas ejected in dehydrating unit in mercuric chleride catalyst production is sent into dust arrester and is carried out dust removal operation, enters heat exchanger subsequently and carries out heat exchange with recovery waste heat, make tail gas be cooled to 40-60 DEG C; Tail gas through recovery waste heat sends into packed tower bottom, enters in tower wash from packed tower bottom, adopts the BaCl of 4-12wt%
2the Ca (OH) of solution, 10-20wt%
2the mixed liquor of solution and 10-20wt% ammoniacal liquor as cleaning solution, BaCl
2solution, Ca (OH)
2the mass ratio of solution and ammoniacal liquor is 6:9:4, and the nozzle of cleaning solution in the middle part of filler tower top and tower carries out spray washing to tower inner exhaust gas respectively, is countercurrent washing in packed tower; Cleaning solution recycles, fresh wash liquid is supplemented after cleaning solution concentration reduces, at packed tower top, offgas outlet arranges adsorbent equipment, tail gas is by emptying after adsorbent equipment, adsorbent is provided with in adsorbent equipment, adsorbent is compound adsorbent, and it consists of the active carbon of 20-60wt%, the y-type zeolite of ZSM-11 and 20-30wt% of 20-40wt%.
Embodiment 4
The tail gas ejected in dehydrating unit in mercuric chleride catalyst production is sent into dust arrester and is carried out dust removal operation, enters heat exchanger subsequently and carries out heat exchange with recovery waste heat, make tail gas be cooled to 40-60 DEG C; Tail gas through recovery waste heat sends into packed tower bottom, enters in tower wash from packed tower bottom, adopts the BaCl of 4-12wt%
2the Ca (OH) of solution, 10-20wt%
2the mixed liquor of solution and 10-20wt% ammoniacal liquor as cleaning solution, BaCl
2solution, Ca (OH)
2the mass ratio of solution and ammoniacal liquor is 5:7:4, and the nozzle of cleaning solution in the middle part of filler tower top and tower carries out spray washing to tower inner exhaust gas respectively, is countercurrent washing in packed tower; Cleaning solution recycles, fresh wash liquid is supplemented after cleaning solution concentration reduces, at packed tower top, offgas outlet arranges adsorbent equipment, tail gas is by emptying after adsorbent equipment, adsorbent is provided with in adsorbent equipment, adsorbent is compound adsorbent, and it consists of the active carbon of 20-60wt%, the y-type zeolite of ZSM-11 and 20-30wt% of 20-40wt%.
Embodiment 5
The tail gas ejected in dehydrating unit in mercuric chleride catalyst production is sent into dust arrester and is carried out dust removal operation, enters heat exchanger subsequently and carries out heat exchange with recovery waste heat, make tail gas be cooled to 40-60 DEG C; Tail gas through recovery waste heat sends into packed tower bottom, enters in tower wash from packed tower bottom, adopts the BaCl of 4-12wt%
2the Ca (OH) of solution, 10-20wt%
2the mixed liquor of solution and 10-20wt% ammoniacal liquor as cleaning solution, BaCl
2solution, Ca (OH)
2the mass ratio of solution and ammoniacal liquor is 6:10:3, and the nozzle of cleaning solution in the middle part of filler tower top and tower carries out spray washing to tower inner exhaust gas respectively, is countercurrent washing in packed tower; Cleaning solution recycles, fresh wash liquid is supplemented after cleaning solution concentration reduces, at packed tower top, offgas outlet arranges adsorbent equipment, tail gas is by emptying after adsorbent equipment, adsorbent is provided with in adsorbent equipment, adsorbent is compound adsorbent, and it consists of the active carbon of 20-60wt%, the y-type zeolite of ZSM-11 and 20-30wt% of 20-40wt%.
Embodiment 6
The tail gas ejected in dehydrating unit in mercuric chleride catalyst production is sent into dust arrester and is carried out dust removal operation, enters heat exchanger subsequently and carries out heat exchange with recovery waste heat, make tail gas be cooled to 40-60 DEG C; Tail gas through recovery waste heat sends into packed tower bottom, enters in tower wash from packed tower bottom, adopts the BaCl of 4-12wt%
2the Ca (OH) of solution, 10-20wt%
2the mixed liquor of solution and 10-20wt% ammoniacal liquor as cleaning solution, BaCl
2solution, Ca (OH)
2the mass ratio of solution and ammoniacal liquor is 5:8:4, and the nozzle of cleaning solution in the middle part of filler tower top and tower carries out spray washing to tower inner exhaust gas respectively, is countercurrent washing in packed tower; Cleaning solution recycles, fresh wash liquid is supplemented after cleaning solution concentration reduces, at packed tower top, offgas outlet arranges adsorbent equipment, tail gas is by emptying after adsorbent equipment, adsorbent is provided with in adsorbent equipment, adsorbent is compound adsorbent, and it consists of the active carbon of 20-60wt%, the y-type zeolite of ZSM-11 and 20-30wt% of 20-40wt%.
Embodiment 7
The tail gas ejected in dehydrating unit in mercuric chleride catalyst production is sent into dust arrester and is carried out dust removal operation, enters heat exchanger subsequently and carries out heat exchange with recovery waste heat, make tail gas be cooled to 40-60 DEG C; Tail gas through recovery waste heat sends into packed tower bottom, enters in tower wash from packed tower bottom, adopts the BaCl of 4-12wt%
2the Ca (OH) of solution, 10-20wt%
2the mixed liquor of solution and 10-20wt% ammoniacal liquor as cleaning solution, BaCl
2solution, Ca (OH)
2the mass ratio of solution and ammoniacal liquor is 4:7:3, and the nozzle of cleaning solution in the middle part of filler tower top and tower carries out spray washing to tower inner exhaust gas respectively, is countercurrent washing in packed tower; Cleaning solution recycles, fresh wash liquid is supplemented after cleaning solution concentration reduces, at packed tower top, offgas outlet arranges adsorbent equipment, tail gas is by emptying after adsorbent equipment, adsorbent is provided with in adsorbent equipment, adsorbent is compound adsorbent, and it consists of the active carbon of 20-60wt%, the y-type zeolite of ZSM-11 and 20-30wt% of 20-40wt%.
Embodiment 8
The tail gas ejected in dehydrating unit in mercuric chleride catalyst production is sent into dust arrester and is carried out dust removal operation, enters heat exchanger subsequently and carries out heat exchange with recovery waste heat, make tail gas be cooled to 40-60 DEG C; Tail gas through recovery waste heat sends into packed tower bottom, enters in tower wash from packed tower bottom, adopts the BaCl of 4-12wt%
2the Ca (OH) of solution, 10-20wt%
2the mixed liquor of solution and 10-20wt% ammoniacal liquor as cleaning solution, BaCl
2solution, Ca (OH)
2the mass ratio of solution and ammoniacal liquor is 6:7:3.5, and the nozzle of cleaning solution in the middle part of filler tower top and tower carries out spray washing to tower inner exhaust gas respectively, is countercurrent washing in packed tower; Cleaning solution recycles, fresh wash liquid is supplemented after cleaning solution concentration reduces, at packed tower top, offgas outlet arranges adsorbent equipment, tail gas is by emptying after adsorbent equipment, adsorbent is provided with in adsorbent equipment, adsorbent is compound adsorbent, and it consists of the active carbon of 20-60wt%, the y-type zeolite of ZSM-11 and 20-30wt% of 20-40wt%.
Embodiment 9
The tail gas ejected in dehydrating unit in mercuric chleride catalyst production is sent into dust arrester and is carried out dust removal operation, enters heat exchanger subsequently and carries out heat exchange with recovery waste heat, make tail gas be cooled to 40-60 DEG C; Tail gas through recovery waste heat sends into packed tower bottom, enters in tower wash from packed tower bottom, adopts the BaCl of 4-12wt%
2the Ca (OH) of solution, 10-20wt%
2the mixed liquor of solution and 10-20wt% ammoniacal liquor as cleaning solution, BaCl
2solution, Ca (OH)
2the mass ratio of solution and ammoniacal liquor is 5:8:3, and the nozzle of cleaning solution in the middle part of filler tower top and tower carries out spray washing to tower inner exhaust gas respectively, is countercurrent washing in packed tower; Cleaning solution recycles, fresh wash liquid is supplemented after cleaning solution concentration reduces, at packed tower top, offgas outlet arranges adsorbent equipment, tail gas is by emptying after adsorbent equipment, adsorbent is provided with in adsorbent equipment, adsorbent is compound adsorbent, and it consists of the active carbon of 20-60wt%, the y-type zeolite of ZSM-11 and 20-30wt% of 20-40wt%.
Claims (1)
1. a purification is in the method for synthesizing the tail gas produced in mercury catalyst, it is characterized in that comprising the following steps: that the tail gas ejected in dehydrating unit in mercuric chleride catalyst production is sent into dust arrester and carried out dust removal operation, enter heat exchanger subsequently and carry out heat exchange with recovery waste heat, make tail gas be cooled to 40-60 DEG C; Tail gas through recovery waste heat sends into packed tower bottom, enters in tower wash from packed tower bottom, adopts the BaCl of 4-12wt%
2the Ca (OH) of solution, 10-20wt%
2the mixed liquor of solution and 10-20wt% ammoniacal liquor as cleaning solution, BaCl
2solution, Ca (OH)
2the mass ratio of solution and ammoniacal liquor is 4-6:7-10:3-4, and the nozzle of cleaning solution in the middle part of filler tower top and tower carries out spray washing to tower inner exhaust gas respectively, is countercurrent washing in packed tower; Cleaning solution recycles, fresh wash liquid is supplemented after cleaning solution concentration reduces, at packed tower top, offgas outlet arranges adsorbent equipment, tail gas is by emptying after adsorbent equipment, adsorbent is provided with in adsorbent equipment, adsorbent is compound adsorbent, and it consists of the active carbon of 20-60wt%, the y-type zeolite of ZSM-11 and 20-30wt% of 20-40wt%.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410617981.4A CN104324598A (en) | 2014-11-05 | 2014-11-05 | Method for purifying tail gas produced in synthesis of mercury catalyst |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410617981.4A CN104324598A (en) | 2014-11-05 | 2014-11-05 | Method for purifying tail gas produced in synthesis of mercury catalyst |
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| CN104324598A true CN104324598A (en) | 2015-02-04 |
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| CN201410617981.4A Pending CN104324598A (en) | 2014-11-05 | 2014-11-05 | Method for purifying tail gas produced in synthesis of mercury catalyst |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105080286A (en) * | 2015-08-11 | 2015-11-25 | 无锡桥阳机械制造有限公司 | Method for removing mercury in mercury-contained tail gas |
| CN110894568A (en) * | 2019-12-20 | 2020-03-20 | 南通辑兴紧固件科技有限公司 | Environment-friendly fastener quenching system and process |
| CN113860331A (en) * | 2021-11-02 | 2021-12-31 | 浙江大洋生物科技集团股份有限公司 | Method for synthesizing high-activity potassium fluoride and co-producing sodium fluoride by using waste liquid as raw material |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101455974A (en) * | 2008-12-29 | 2009-06-17 | 万山特区红晶汞业有限公司 | Tail-gas comprehensive utilization method in mercuric chloride catalyst |
-
2014
- 2014-11-05 CN CN201410617981.4A patent/CN104324598A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101455974A (en) * | 2008-12-29 | 2009-06-17 | 万山特区红晶汞业有限公司 | Tail-gas comprehensive utilization method in mercuric chloride catalyst |
Non-Patent Citations (1)
| Title |
|---|
| 路乘风等: "《防尘防毒技术》", 31 May 2004, 化学工业出版社 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105080286A (en) * | 2015-08-11 | 2015-11-25 | 无锡桥阳机械制造有限公司 | Method for removing mercury in mercury-contained tail gas |
| CN110894568A (en) * | 2019-12-20 | 2020-03-20 | 南通辑兴紧固件科技有限公司 | Environment-friendly fastener quenching system and process |
| CN113860331A (en) * | 2021-11-02 | 2021-12-31 | 浙江大洋生物科技集团股份有限公司 | Method for synthesizing high-activity potassium fluoride and co-producing sodium fluoride by using waste liquid as raw material |
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Application publication date: 20150204 |
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