CN206688471U - One kind recovery HCl and Cl2Device - Google Patents
One kind recovery HCl and Cl2Device Download PDFInfo
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- CN206688471U CN206688471U CN201720268404.8U CN201720268404U CN206688471U CN 206688471 U CN206688471 U CN 206688471U CN 201720268404 U CN201720268404 U CN 201720268404U CN 206688471 U CN206688471 U CN 206688471U
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- Prior art keywords
- hcl
- tower
- absorption
- desorption
- gas
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- 238000011084 recovery Methods 0.000 title claims abstract description 8
- 238000010521 absorption reaction Methods 0.000 claims abstract description 123
- 238000003795 desorption Methods 0.000 claims abstract description 65
- 239000002250 absorbent Substances 0.000 claims abstract description 27
- 230000002745 absorbent Effects 0.000 claims abstract description 23
- 239000007788 liquid Substances 0.000 claims description 28
- 238000000034 method Methods 0.000 claims description 21
- 239000003960 organic solvent Substances 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- VZGDMQKNWNREIO-UHFFFAOYSA-N tetrachloromethane Chemical compound ClC(Cl)(Cl)Cl VZGDMQKNWNREIO-UHFFFAOYSA-N 0.000 claims description 4
- 239000006096 absorbing agent Substances 0.000 claims description 3
- KEQGZUUPPQEDPF-UHFFFAOYSA-N 1,3-dichloro-5,5-dimethylimidazolidine-2,4-dione Chemical compound CC1(C)N(Cl)C(=O)N(Cl)C1=O KEQGZUUPPQEDPF-UHFFFAOYSA-N 0.000 claims description 2
- XTHPWXDJESJLNJ-UHFFFAOYSA-N chlorosulfonic acid Substances OS(Cl)(=O)=O XTHPWXDJESJLNJ-UHFFFAOYSA-N 0.000 claims description 2
- PXJJSXABGXMUSU-UHFFFAOYSA-N disulfur dichloride Chemical compound ClSSCl PXJJSXABGXMUSU-UHFFFAOYSA-N 0.000 claims description 2
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 127
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 119
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 119
- 239000000460 chlorine Substances 0.000 description 91
- 239000007789 gas Substances 0.000 description 19
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 6
- 230000003647 oxidation Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 2
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 2
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 description 2
- 150000001298 alcohols Chemical class 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 150000002148 esters Chemical class 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 150000002576 ketones Chemical class 0.000 description 2
- XNLICIUVMPYHGG-UHFFFAOYSA-N pentan-2-one Chemical compound CCCC(C)=O XNLICIUVMPYHGG-UHFFFAOYSA-N 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 239000005708 Sodium hypochlorite Substances 0.000 description 1
- KXKVLQRXCPHEJC-UHFFFAOYSA-N acetic acid trimethyl ester Natural products COC(C)=O KXKVLQRXCPHEJC-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000009713 electroplating Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 150000002170 ethers Chemical class 0.000 description 1
- WBJINCZRORDGAQ-UHFFFAOYSA-N formic acid ethyl ester Natural products CCOC=O WBJINCZRORDGAQ-UHFFFAOYSA-N 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
One kind recovery HCl and Cl2Device, include the Cl of connection2Absorption plant, HCl absorption plants；Cl2Absorption plant is also associated with Cl2Desorption apparatus, HCl absorption plants are also associated with HCl desorption apparatus；Wherein, Cl2Absorption plant includes Cl2Absorption tower, HCl absorption plants include at least one HCl absorption towers, Cl2Desorption apparatus includes Cl2Desorber, Cl2The middle part connection Cl of desorber2Absorption tower, HCl desorption apparatus include HCl desorbers, the middle part connection first order HCl absorption towers of HCl desorbers.The beneficial effect of the device：HCl and Cl2The rate of recovery it is high, absorbent is repeatable to be utilized, and is avoided environmental pollution, is reduced production cost, increase economic efficiency.
Description
Technical Field
The utility model relates to a retrieve HCl and Cl2Belonging to the technical field of material separation in chemical engineering.
Background
The hydrogen chloride and chlorine waste gas are inevitably generated in the industries of chemical industry, paper making, electroplating, grease and the like, and if purification measures are not taken, the concentration of the hydrogen chloride waste gas in the air of a workshop can reach dozens of even dozens ofHundreds of mg/m to 3, which is far higher than the environmental sanitation standard of 0.3mg/m to 3. For containing HCl and Cl industrially2The method for treating tail gas of other non-condensable gas comprises the following steps: first, oxidation of HCl to Cl2Such as electrolysis, direct oxidation, catalytic oxidation, but the oxidation process is complicated and energy consumption is too high, and Cl is generated2Still further processing is required. Secondly, absorbing hydrogen chloride gas in the tail gas to prepare hydrochloric acid (the pressurized gas is used for purging chlorine in the hydrochloric acid); then drying the chlorine gas, cooling and liquefying the chlorine gas, and recycling the chlorine gas. The third idea is that most of chlorine gas is first recovered by freezing and then hydrochloric acid and sodium hypochlorite are made by alkali liquor absorption method by utilizing the difference of freezing points of chlorine gas and hydrogen chloride, but the method has high requirements on temperature and instrument conditions and consumes much energy.
SUMMERY OF THE UTILITY MODEL
The utility model discloses not enough to prior art exists provides a retrieve HCl and Cl2The device can simplify the absorption equipment and the process flow in the prior art and improve the recovery rate.
Wherein, the utility model provides a technical scheme as follows of above-mentioned technical problem:
HCl and Cl recovery2In the order of separation, the device comprising in succession the linking of Cl2An absorption apparatus, an HCl absorption apparatus, the Cl2The absorption device is also connected with Cl2The HCl absorption device is also connected with an HCl desorption device; wherein,
the Cl2The absorption means comprises Cl2Absorption column, Cl2The tower kettle of the absorption tower is communicated with the top outlet of the gas-liquid filter;
the HCl absorption device comprises an HCl absorption tower, and a tower kettle of the HCl absorption tower is communicated with Cl2A top outlet of the absorber column;
the Cl2The desorption apparatus comprises Cl2A desorption tower is arranged in the reaction kettle,Cl2the desorption tower is communicated with Cl2An absorption tower;
the HCl desorption device comprises an HCl desorption tower which is communicated with an HCl absorption tower;
the Cl2Cl in absorption column2The absorbent is one of sulfur monochloride, chlorosulfonic acid, carbon tetrachloride and other organic solvents with similar properties, the HCl absorbent in the HCl absorption tower is one of organic solvents, such as alcohols, ketones, esters, ethers and other organic solvents, the alcohols comprise methanol, ethanol, isopropanol, butanol and the like, the ketones comprise acetone, butanone, 2-pentanone and the like, and the esters comprise ethyl formate, methyl acetate and the like.
Further, the Cl2The absorption device is also connected with a gas-liquid filter for filtering water and other condensate in the tail gas; by Cl2The tower kettle of the absorption tower is communicated with the top outlet of the gas-liquid filter.
Further, the gas-liquid filter is a gas-liquid filter with a wire mesh demister.
Further, the HCl absorption tower is at least one stage; when a multistage HCl absorption tower exists, the HCl desorption tower is communicated with the first-stage HCl absorption tower, the multistage HCl absorption towers are connected in series, the top of the front-stage HCl absorption tower is communicated with the tower kettle of the rear-stage absorption tower, the adjacent HCl absorption towers are communicated by a circulating pipeline, the tower kettle of the HCl desorption tower is connected with an HCl absorbent buffer tank, and the HCl absorbent buffer tank is connected with the last-stage HCl absorption tower through a pipeline.
Further, the Cl2And circulating pumps and coolers are arranged on pipelines between the top of the absorption tower and the tower kettle and between the top of the HCl absorption tower and the tower kettle.
Further, the Cl2The tower kettle of the desorption tower is connected with Cl2Reboiler and Cl2Absorbent buffer tank, said Cl2The absorbent buffer tank is connected with Cl through a pipeline2An absorption tower.
Further, the Cl2The top of the desorption tower is filled with Cl2Overhead condenser, Cl2Cl is arranged below the tower top condenser2Product surge tank, Cl2The output end of the product buffer tank is connected with Cl2The top of the desorption tower.
Furthermore, the tower kettle of the HCl desorption tower is connected with an HCl reboiler, an HCl tower top condenser is arranged at the top of the HCl desorption tower, an HCl product buffer tank is arranged below the HCl tower top condenser, and the output end of the HCl product buffer tank is connected with the top of the HCl desorption tower.
Further, an inlet is formed in the gas-liquid filter, a gas outlet is formed in the top of the gas-liquid filter, and a liquid outlet is formed in the bottom of the gas-liquid filter.
HCl and Cl recovery2The method comprises the following steps:
(1) absorption of
Tail gas from Cl2The absorption tower enters the tower kettle and passes through Cl2Absorption in an absorption column, saturated Cl2From Cl in solution2The desorption tower enters, the gas enters a first-stage HCl absorption tower, and the saturated HCl solution in the first-stage HCl absorption tower enters the HCl desorption tower;
(2) desorption of
Cl2The desorption tower is pressurized and saturated with Cl2After the solution is subjected to a heat and mass transfer process, Cl2Conversion to gas phase rising to Cl2At the top of the desorber in Cl2Condensing the top of the desorption tower into liquid to obtain Cl2The product, a small amount of uncondensed gas which is not condensed is safely discharged, and part of Cl2Liquid from Cl2Refluxing the top of the desorption tower into the tower to remove Cl2Absorbent quilt Cl2Liquid cooling and condensing in Cl2Obtaining Cl at the bottom of the desorption tower2An absorbent product;
the method comprises the following steps that pressurization operation is carried out in an HCl desorption tower, HCl is converted into a gas phase to ascend to the top of the HCl desorption tower after a saturated HCl solution is subjected to a heat and mass transfer process, the gas phase is condensed into liquid through an HCl tower top condenser, an HCl product is obtained, a small amount of uncondensed gas is safely discharged, part of HCl liquid flows back into the HCl desorption tower from the top of the HCl desorption tower, an HCl absorbent is cooled by the HCl liquid, and the HCl absorbent product is obtained in the bottom of the HCl desorption tower.
Further, the tail gas enters Cl2Filtering and separating before the absorption tower: introducing tail gas into gas-liquid filter, discharging condensate containing HCl and Cl2、N2Is discharged from the upper part of the gas-liquid filter and is discharged from Cl2Cl entering the tower kettle of the absorption tower2An absorption tower.
Further, in the step (1), unabsorbed tail gas discharged from the top of the first-stage HCl absorption tower enters the next-stage HCl absorption tower and finally enters the last HCl absorption tower, and the unsaturated solution obtained in each stage of HCl absorption tower returns to the previous-stage HCl absorption tower; each of the HCl absorption towers, Cl2The pipeline between the top of the absorption tower and the tower kettle is provided with a circulating pump and a cooler, and for each HCl absorption tower, the solution circulates between the inside of each HCl absorption tower and the cooler through the circulating pump and Cl2Circulation in the absorption tower and between the coolers.
Further, in the step (3), in Cl2Cl obtained from tower kettle of desorption tower2Introduction of absorbent product into Cl2Recycling in the absorption tower; introducing the HCl absorbent product obtained from the tower kettle of the HCl desorption tower into a second-stage HCl absorption tower for cyclic utilization.
Further, the Cl2The tower kettle of the desorption tower is connected with Cl2Reboiler and Cl2Absorbent buffer tank, said Cl2Cl is arranged below the tower top condenser2Product surge tank, Cl2The output end of the product buffer tank is connected with Cl through a pump2The top of the desorption tower; the HCl desorption tower is characterized in that an HCl reboiler and an HCl absorbent buffer tank are connected to the tower kettle of the HCl desorption tower, an HCl product buffer tank is arranged below an HCl tower top condenser, and the output end of the HCl product buffer tank is connected to the top of the HCl desorption tower.
The utility model provides a process method and device's beneficial effect is: (1) will be provided withHCl and Cl2In the process of recycling, the absorbent can be recycled, thereby avoiding the environmental pollution caused by emission, reducing the production cost and improving the economic benefit; (2) the absorbent absorbs HCl and Cl2The tail gas of the absorption tower is HCl and Cl discharged in an exothermic process due to overhigh temperature in the absorption tower2The secondary tail gas is increased, the absorption effect is reduced, a cooler is additionally arranged behind the circulating pump, the temperature of the solution is reduced, and the low-temperature solution directly contacts the high-temperature solution to achieve the purpose of reducing the temperature in the absorption tower; (3) HCl and Cl2Is completely separated, HCl and Cl2The recovery rate is high and can reach more than 99.9 percent; (4) the utility model discloses very high practical value and very big market needs have.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention;
fig. 2 is a schematic structural diagram of an embodiment of the present invention.
Wherein, the gas-liquid filter 1; cl2An absorption tower 2; a first-stage HCl absorption tower 3-1; a second stage HCl absorber 3-2; a third-stage HCl absorption tower 3-3; cl2A desorption tower 4; an HCl desorption tower 5; a circulation pump 6; a cooler 7; cl2A reboiler 8; cl2An absorbent buffer tank 9; cl2An overhead condenser 10; cl2A product surge tank 11; an HCl reboiler 12; an HCl absorbent buffer tank 13; an HCl overhead condenser 14; HCl product surge tank 15.
Detailed Description
The principles and features of the present invention are described below in conjunction with the following drawings, the examples given are only intended to illustrate the present invention and are not intended to limit the scope of the present invention.
Example 1
FIG. 1, a process for recovering HCl and Cl2The device comprising in sequence, according to the separation order, connected Cl2An absorption tower 2 and two-stage HCl absorption towers which are numbered as a first-stage HCl absorption tower 3-1 and a second-stage HCl absorption tower 3-2, wherein a tower kettle of the first-stage HCl absorption tower 3-1 is communicated with Cl2The top outlet of the absorption tower 2, the tower kettle of the second-stage HCl absorption tower 3-2 are communicated with the top outlet of the first-stage HCl absorption tower 3-1, and Cl2The absorption tower 2 is also connected with Cl2The middle part of the desorption tower 4 and the first-stage HCl absorption tower 3-1 are also connected with the middle part of the HCl desorption tower 5, and the device can be divided into two systems on the whole: cl2Absorption and desorption system, HCl absorption and desorption system, Cl2The tower 2 kettle of the absorption tower is filled with Cl2The absorption agent, the first-stage HCl absorption tower 3-1 and the second-stage HCl absorption tower 3-2 are filled with HCl absorption agent.
First, Cl2The absorption and desorption systems are as follows:
Cl2a circulating pump 6 and a cooler 7 are arranged on pipelines between the top of the absorption tower 2 and the tower kettle; cl2The tower kettle 4 of the desorption tower is connected with Cl2Reboiler 8 and Cl2Absorbent buffer tank 9, Cl2The top of the desorption tower 4 is filled with Cl2Overhead condenser 10, Cl2Cl is arranged below the tower top condenser 102Product surge tank 11, Cl2The output end of the product buffer tank 11 is connected with Cl through a pump2The top of the desorption tower 4.
Secondly, the HCl absorption and desorption system is as follows:
a circulating pump 6 and a cooler 7 are arranged on pipelines between the top of the first-stage HCl absorption tower 3-1 and the tower kettle; the tower kettle of the HCl desorption tower 5 is connected with an HCl reboiler 12 and an HCl absorbent buffer tank 13, an HCl tower top condenser 14 is arranged at the tower top of the HCl desorption tower 5, an HCl product buffer tank 15 is arranged below the HCl tower top condenser 14, and the output end of the HCl product buffer tank 15 is connected with the tower top of the HCl desorption tower 5.
The material circulation between the first-stage HCl absorption tower 3-1 and the second-stage HCl absorption tower 3-2 and the material transportation are realized by arranging a remote transmission liquid level meter interlocking regulating valve and a flow meter interlocking regulating valve or a remote transmission liquid level meter and a flow meter interlocking regulating valve on a circuit.
Example 2
As shown in FIG. 2, Cl was added in the base of example 12The absorption tower 2 is also connected with a gas-liquid filter 1, and in addition, the number of the HCl absorption towers is three, namely a first-stage HCl absorption tower 3-1, a second-stage HCl absorption tower 3-2 and a third-stage HCl absorption tower 3-3.
The above description is only for the preferred embodiment of the present invention, and is not intended to limit the present invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included within the protection scope of the present invention.
Claims (8)
1. HCl and Cl recovery2Characterized in that the device comprises, in order of separation, a linking Cl2An absorption apparatus, an HCl absorption apparatus, the Cl2The absorption device is also connected with Cl2The HCl absorption device is also connected with an HCl desorption device; wherein,
the Cl2The absorption means comprises Cl2Absorption column, Cl2The tower kettle of the absorption tower is communicated with the top outlet of the gas-liquid filter;
the HCl absorption device comprises an HCl absorption tower and an HCl absorption towerThe tower kettle is communicated with Cl2A top outlet of the absorber column;
the Cl2The desorption apparatus comprises Cl2Desorption column, Cl2The desorption tower is communicated with Cl2An absorption tower;
the HCl desorption device comprises an HCl desorption tower which is communicated with an HCl absorption tower;
the Cl2Cl in absorption column2The absorbent comprises one of sulfur monochloride, chlorosulfonic acid and carbon tetrachloride, and the HCl absorbent in the HCl absorption tower is an organic solvent.
2. A process for recovering HCl and Cl as in claim 12Characterized in that said Cl is2The absorption device is also connected with a gas-liquid filter which passes Cl2The tower kettle of the absorption tower is communicated with the top outlet of the gas-liquid filter.
3. A process for recovering HCl and Cl as in claim 12The device is characterized in that the HCl absorption tower is at least one stage; when a multistage HCl absorption tower exists, the HCl desorption tower is communicated with the first-stage HCl absorption tower, the multistage HCl absorption towers are connected in series, the top of the front-stage HCl absorption tower is communicated with the tower kettle of the rear-stage absorption tower, the adjacent HCl absorption towers are communicated by a circulating pipeline, the tower kettle of the HCl desorption tower is connected with an HCl absorbent buffer tank, and the HCl absorbent buffer tank is connected with the last-stage HCl absorption tower through a pipeline.
4. A process for recovering HCl and Cl as in claim 12Characterized in that said Cl is2And circulating pumps and coolers are arranged on pipelines between the top of the absorption tower and the tower kettle and between the top of the HCl absorption tower and the tower kettle.
5. A process for recovering HCl and Cl as in claim 12Characterized in that said Cl is2The tower kettle of the desorption tower is connected with Cl2Reboiler and Cl2An absorbent buffer tank is arranged in the absorption tank,the Cl2The absorbent buffer tank is connected with Cl through a pipeline2An absorption tower.
6. A process for recovering HCl and Cl according to claim 1 or 52Characterized in that said Cl is2The top of the desorption tower is filled with Cl2Overhead condenser, Cl2Cl is arranged below the tower top condenser2Product surge tank, Cl2The output end of the product buffer tank is connected with Cl2The top of the desorption tower.
7. A process for recovering HCl and Cl according to claim 1 or 32The device is characterized in that an HCl reboiler is connected with a tower kettle of the HCl desorption tower, an HCl tower top condenser is arranged at the top of the HCl desorption tower, an HCl product buffer tank is arranged below the HCl tower top condenser, and the output end of the HCl product buffer tank is connected with the top of the HCl desorption tower.
8. A process for recovering HCl and Cl as set forth in claim 22The device is characterized in that the gas-liquid filter is provided with an inlet, the top of the gas-liquid filter is provided with a gas outlet, and the bottom of the gas-liquid filter is provided with a liquid outlet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720268404.8U CN206688471U (en) | 2017-03-17 | 2017-03-17 | One kind recovery HCl and Cl2Device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720268404.8U CN206688471U (en) | 2017-03-17 | 2017-03-17 | One kind recovery HCl and Cl2Device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206688471U true CN206688471U (en) | 2017-12-01 |
Family
ID=60443665
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720268404.8U Active CN206688471U (en) | 2017-03-17 | 2017-03-17 | One kind recovery HCl and Cl2Device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206688471U (en) |
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2017
- 2017-03-17 CN CN201720268404.8U patent/CN206688471U/en active Active
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