CN102258935A - Recovery and utilization method of phosgene in phosgenation reaction tail gas - Google Patents
Recovery and utilization method of phosgene in phosgenation reaction tail gas Download PDFInfo
- Publication number
- CN102258935A CN102258935A CN2011101012604A CN201110101260A CN102258935A CN 102258935 A CN102258935 A CN 102258935A CN 2011101012604 A CN2011101012604 A CN 2011101012604A CN 201110101260 A CN201110101260 A CN 201110101260A CN 102258935 A CN102258935 A CN 102258935A
- Authority
- CN
- China
- Prior art keywords
- phosgene
- reaction tower
- phosgenation
- product
- tail gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- YGYAWVDWMABLBF-UHFFFAOYSA-N Phosgene Chemical compound ClC(Cl)=O YGYAWVDWMABLBF-UHFFFAOYSA-N 0.000 title claims abstract description 142
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 66
- 238000011084 recovery Methods 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 17
- 239000007789 gas Substances 0.000 claims abstract description 47
- 239000007788 liquid Substances 0.000 claims abstract description 22
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000004064 recycling Methods 0.000 claims abstract description 10
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 8
- 230000003134 recirculating effect Effects 0.000 claims description 59
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 230000004044 response Effects 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 2
- 238000009833 condensation Methods 0.000 claims description 2
- 238000007664 blowing Methods 0.000 abstract 1
- 230000006378 damage Effects 0.000 description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000003912 environmental pollution Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 208000027418 Wounds and injury Diseases 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 2
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 2
- 208000014674 injury Diseases 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- XMJHPCRAQCTCFT-UHFFFAOYSA-N methyl chloroformate Chemical compound COC(Cl)=O XMJHPCRAQCTCFT-UHFFFAOYSA-N 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 238000006552 photochemical reaction Methods 0.000 description 1
- 230000000192 social effect Effects 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to a recovery and utilization method of phosgene in phosgenation reaction tail gas. According to the method, phosgene tail gas containing 5.5% of phosgene is delivered to a first phosgene recovering reaction tower, a recycling liquid in a first circulation vessel is delivered to the first phosgene recovering reaction tower through a first circulation pump, such that a phosgenated product is produced through a reaction between the phosgene tail gas and the recycling liquid, and the product is delivered to the first circulation vessel; gas delivered from the first phosgene recovering reaction tower is delivered to a second phosgene recovering reaction tower, a recycling liquid in a second circulation vessel is delivered to the second phosgene recovering reaction tower through a second circulation pump, such that a phosgenated product is produced through a reaction between the phosgene tail gas and the recycling liquid, and the product is delivered to the second circulation vessel; When the concentration of the phosgenated product in the first circulation vessel reaches 98%, the phosgenated product in the first circulation vessel is delivered to a deacidification vessel. When a nitrogen blowing standard is reached, the finished phosgenated product is obtained. Phosgenation tail gas containing 0.5% of phosgene is delivered from the second phosgene recovering reaction tower to a condenser, and then delivered to a phosgenation tail gas system containing 0.5% of phosgene through a buffer. According to the invention, a phosgenated product is produced from phosgene in phosgenation tail gas, and phosgene content is reduced from 5.5% to 0.5%.
Description
Technical field
The present invention relates to the recoverying and utilizing method of phosgene in a kind of phosgenation reaction tail gas.
Background technology
At present, the tail gas treatment process of all phosgenation products behind logical phosgene reaction all adopts following technical process: at first phosgene tail gas sponges the hydrogen chloride that produces in the photochemical reaction through water and reclaims hydrochloric acid, enter three grades of SN-7501 molecular sieve filling towers then and carry out hot water catalysis destruction, phosgene is broken to hydrogen chloride and carbon dioxide recovery hydrochloric acid, and then enter caustic wash tower and destroy remaining phosgene with NaOH, simultaneously behind the absorbing carbon dioxide, by being higher than the emptying of the high row of 40m exhaust duct.The destruction of this technology phosgene tail gas, concentration of emission, rate of discharge can satisfy " discharge standard of air pollutants ".But only solved the destruction of phosgene tail gas, and failed to utilize the phosgene in the tail gas.If the generation operation is unexpected in logical light process of producing product, perhaps generation hot water catalysis destruction is not thorough when handling the higher concentration phosgene, just the discharging that can exceed standard causes environmental pollution, personnel is damaged.
Summary of the invention
The objective of the invention is to overcome the deficiency that prior art exists, the recoverying and utilizing method of phosgene in a kind of phosgenation reaction tail gas is provided.
Purpose of the present invention is achieved through the following technical solutions:
The recoverying and utilizing method of phosgene in the phosgenation reaction tail gas, characteristics are: recycling system comprises that first phosgene reclaims reaction tower, second phosgene reclaims reaction tower, first recirculating still, second recirculating still, first circulating pump, second circulating pump and depickling still, reclaim reaction tower at first phosgene, second phosgene reclaims reaction tower, drop in first recirculating still and second recirculating still and reclaim liquid, come the phosgene tail gas that contains phosgene 5.5% of self-contained phosgene 5.5% phosgene exhaust system to enter first phosgene recovery reaction tower, by first circulating pump recovery liquid in first recirculating still is delivered to first phosgene and reclaim reaction tower, the phosgene that reclaims in the liquid and first phosgene recovery reaction tower reacts generation phosgenation product, the phosgenation product exports first recirculating still to, along with circulation and temperature control, the phosgenation product design constantly raises in first recirculating still;
The gas that comes out from first phosgene recovery reaction tower enters second phosgene recovery reaction tower, second circulating pump is delivered to second phosgene with the recovery liquid in second recirculating still and is reclaimed reaction tower, the phosgene that reclaims in the liquid and second phosgene recovery reaction tower reacts generation phosgenation product, the phosgenation product exports second recirculating still to, along with circulation and temperature control, the phosgenation product design constantly raises in second recirculating still;
The phosgenation product design reaches at 98% o'clock in first recirculating still, and the phosgenation transferred product in first recirculating still to the depickling still, is carried out nitrogen by nitrogen pot and blown drum back up to standard acquisition phosgenation product, and the phosgenation product is delivered to phosgenation product holding vessel;
Phosgenation product in first recirculating still will continue circular response in phosgenation transferred product to the first recirculating still in second recirculating still after shifting, it is 40～50% that second recirculating still shifts the phosgenation product design of coming; When second recirculating still is empty, replenish the new recovery liquid of adding by reclaiming flow container to second recirculating still, so repeatedly;
Second phosgene reclaims the phosgene tail gas that reaction tower output contains phosgene 0.5%, and the phosgene tail gas that contains phosgene 0.5% enters to deliver to through buffer after the condenser condenses again and contains phosgene 0.5% phosgene exhaust system.
The recoverying and utilizing method of phosgene in the above-mentioned phosgenation reaction tail gas, described first phosgene reclaim reaction tower and second phosgene recovery reaction tower is the tower reaction tower of film absorption.
The invention has the advantages that:
The present invention is provided with recycling system by enter the destruction tower at phosgene tail gas before, the phosgene that makes full use of in the phosgene tail gas is made the phosgenation product, effectively reduce the phosgene amount that contains that enters phosgene tail gas breaking plant, be reduced to 0.5% with containing the phosgene amount in the phosgene tail gas from 5.5%, reduced the load of the system that destroys, utilize phosgene manufacturing in the phosgene tail gas to obtain quality and reclaim product greater than 98% phosgene, effectively reduce and enter phosgene content in the classical phosgene exhaust gas processing device, under any circumstance all guaranteed the qualified discharge of phosgene tail gas, thoroughly stopped environmental pollution and to the generation of personnel's injury accident, improve security, prevented the accident generation.This process economics benefit and social effect are remarkable, can be rated as have novelty, the good technology of creativeness, practicality.
Description of drawings
Fig. 1: the organigram of recycling system of the present invention.
The implication of each Reference numeral among the figure:
1-contains phosgene 5.5% phosgene exhaust system; 2-first phosgene reclaims reaction tower; 3-second phosgene reclaims reaction tower; The 4-condenser; 5-contains phosgene 0.5% phosgene exhaust system; The 6-surge tank; 7-reclaims flow container; 8-depickling still; 9-first recirculating still; 10-second recirculating still; 11-first circulating pump; 12-second circulating pump; 13-phosgenation product holding vessel; The 14-nitrogen pot.
The specific embodiment
The recoverying and utilizing method of phosgene in the phosgenation reaction tail gas, as shown in Figure 1, recycling system comprises that first phosgene reclaims reaction tower 2, second phosgene reclaims reaction tower 3, first recirculating still 9, second recirculating still 10, first circulating pump 11, second circulating pump 12 and depickling still 8, reclaim reaction tower 2 at first phosgene, second phosgene reclaims reaction tower 3, drop in first recirculating still 9 and second recirculating still 10 and reclaim liquid, come the phosgene tail gas that contains phosgene 5.5% of self-contained phosgene 5.5% phosgene exhaust system 1 to enter first phosgene recovery reaction tower 2, by first circulating pump 11 the recovery liquid in first recirculating still 9 is delivered to first phosgene and reclaim reaction tower 2, the phosgene that reclaims in the liquid and first phosgene recovery reaction tower 2 reacts generation phosgenation product, the phosgenation product exports first recirculating still 9 to, along with circulation and temperature control, the phosgenation product design constantly raises in first recirculating still 9;
The gas that comes out from first phosgene recovery reaction tower 2 enters second phosgene recovery reaction tower 3, second circulating pump 12 is delivered to second phosgene with the recovery liquid in second recirculating still 10 and is reclaimed reaction tower 3, the phosgene that reclaims in the liquid and second phosgene recovery reaction tower 3 reacts generation phosgenation product, the phosgenation product exports second recirculating still 10 to, along with circulation and temperature control, the phosgenation product design constantly raises in second recirculating still 10;
When the phosgenation product design reaches 98% in first recirculating still 9, with the phosgenation transferred product in first recirculating still 9 to depickling still 8, carry out nitrogen by nitrogen pot 14 and blow drum back up to standard acquisition phosgenation product, the phosgenation product is delivered to phosgenation product holding vessel 13;
Phosgenation product in first recirculating still 9 will continue circular response in phosgenation transferred product to the first recirculating still 9 in second recirculating still 10 after shifting, it is 40～50% that second recirculating still 10 shifts the phosgenation product design of coming; When second recirculating still, 10 skies, replenish the new recovery liquid of adding by reclaiming flow container 7 to second recirculating still 10, so repeatedly;
Second phosgene reclaims the phosgene tail gas that reaction tower 3 outputs contain phosgene 0.5%, and the phosgene tail gas that contains phosgene 0.5% enters to deliver to through buffer 6 after condenser 4 condensations again and contains phosgene 0.5% phosgene exhaust system 5.
Wherein, first phosgene recovery reaction tower 2 and second phosgene recovery reaction tower 3 are the tower reaction tower of film absorption.First recirculating still 9 and second recirculating still 10 are recirculating stills that low-speed agitator and cooling system are installed, and material is determined with the requirement of phosgenation product.
The actual consumption data contrast on the methylchloroformate production line of process of the present invention and traditional handicraft method is as follows:
The present invention is provided with recycling system by enter the destruction tower at phosgene tail gas before, the phosgene that makes full use of in the phosgene tail gas is made the phosgenation product, effectively reduce the phosgene amount that contains that enters phosgene tail gas breaking plant, be reduced to 0.5% with containing the phosgene amount in the phosgene tail gas from 5.5%, reduced the load of the system that destroys, utilize phosgene manufacturing in the phosgene tail gas to obtain quality and reclaim product greater than 98% phosgene, effectively reduce and enter phosgene content in the classical phosgene exhaust gas processing device, under any circumstance all guaranteed the qualified discharge of phosgene tail gas, thoroughly stopped environmental pollution and to the generation of personnel's injury accident, improve security, prevented the accident generation.
The above only is a preferred implementation of the present invention, for those skilled in the art, under the prerequisite that does not break away from the principle of the invention, can also make some improvements and modifications, and these improvements and modifications also should be considered as protection scope of the present invention.
Claims (2)
1. the recoverying and utilizing method of phosgene in the phosgenation reaction tail gas, it is characterized in that: recycling system comprises that first phosgene reclaims reaction tower (2), second phosgene reclaims reaction tower (3), first recirculating still (9), second recirculating still (10), first circulating pump (11), second circulating pump (12) and depickling still (8), reclaim reaction tower (2) at first phosgene, second phosgene reclaims reaction tower (3), drop in first recirculating still (9) and second recirculating still (10) and reclaim liquid, come the phosgene tail gas that contains phosgene 5.5% of self-contained phosgene 5.5% phosgene exhaust system (1) to enter first phosgene recovery reaction tower (2), by first circulating pump (11) the recovery liquid in first recirculating still (9) is delivered to first phosgene and reclaim reaction tower (2), the phosgene that reclaims in the liquid and first phosgene recovery reaction tower (2) reacts generation phosgenation product, the phosgenation product exports first recirculating still (9) to, along with circulation and temperature control, the phosgenation product design constantly raises in first recirculating still (9);
The gas that comes out from first phosgene recovery reaction tower (2) enters second phosgene recovery reaction tower (3), second circulating pump (12) is delivered to second phosgene with the recovery liquid in second recirculating still (10) and is reclaimed reaction tower (3), the phosgene that reclaims in the liquid and second phosgene recovery reaction tower (3) reacts generation phosgenation product, the phosgenation product exports second recirculating still (10) to, along with circulation and temperature control, the phosgenation product design constantly raises in second recirculating still (10);
The phosgenation product design reaches at 98% o'clock in first recirculating still (9), with the phosgenation transferred product in first recirculating still (9) to depickling still (8), carry out nitrogen by nitrogen pot (14) and blow drum back up to standard acquisition phosgenation product, the phosgenation product is delivered to phosgenation product holding vessel (13);
Phosgenation product in first recirculating still (9) will continue circular response in phosgenation transferred product to the first recirculating still (9) in second recirculating still (10) after shifting, it is 40～50% that second recirculating still (10) shifts the phosgenation product design of coming; When second recirculating still (10) is empty, replenish the new recovery liquid of adding by reclaiming flow container (7) to second recirculating still (10), so repeatedly;
Second phosgene reclaims the phosgene tail gas that reaction tower (3) output contains phosgene 0.5%, and the phosgene tail gas that contains phosgene 0.5% enters to deliver to through buffer (6) after condenser (4) condensation again and contains phosgene 0.5% phosgene exhaust system (5).
2. the recoverying and utilizing method of phosgene in the phosgenation reaction tail gas according to claim 1 is characterized in that: described first phosgene reclaims reaction tower (2) and second phosgene recovery reaction tower (3) is the tower reaction tower of film absorption.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101012604A CN102258935A (en) | 2011-04-22 | 2011-04-22 | Recovery and utilization method of phosgene in phosgenation reaction tail gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101012604A CN102258935A (en) | 2011-04-22 | 2011-04-22 | Recovery and utilization method of phosgene in phosgenation reaction tail gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102258935A true CN102258935A (en) | 2011-11-30 |
Family
ID=45005884
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011101012604A Pending CN102258935A (en) | 2011-04-22 | 2011-04-22 | Recovery and utilization method of phosgene in phosgenation reaction tail gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102258935A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105289247A (en) * | 2015-10-20 | 2016-02-03 | 安徽广信农化股份有限公司 | Stearoyl chloride phosgene recovery method |
| CN106008268A (en) * | 2016-05-18 | 2016-10-12 | 江苏蓝丰生物化工股份有限公司 | Method for recycling phosgene in tail gas produced through thermo-optical reaction for synthesis of 3,5-dichlorophenyl isocyanate |
| CN111686556A (en) * | 2020-07-31 | 2020-09-22 | 济宁康盛彩虹生物科技有限公司 | Industrial treatment system and treatment method for solid light tail gas in process of synthesizing fluorinated phase transfer catalyst |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1547482A (en) * | 1975-07-15 | 1979-06-20 | Basf Ag | Removal of phosgene from off-gas |
| CN101018596A (en) * | 2004-09-13 | 2007-08-15 | 巴斯福股份公司 | Method for separating hydrogen chloride and phosgene |
| CN101348252A (en) * | 2008-04-25 | 2009-01-21 | 甘肃银光化学工业集团有限公司 | Phosgene recovery method for toluene diisocyanate production process |
| CN101348446A (en) * | 2008-04-25 | 2009-01-21 | 甘肃银光化学工业集团有限公司 | Phosgene removing method for TDI production |
| US20090104099A1 (en) * | 2007-10-17 | 2009-04-23 | Au-Yeung Patrick H | Rich gas absorption apparatus and method |
| CN101671273A (en) * | 2009-09-18 | 2010-03-17 | 天津大学 | Method for recycling phosgene in continuous production process of toluene di-isocyanate |
-
2011
- 2011-04-22 CN CN2011101012604A patent/CN102258935A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1547482A (en) * | 1975-07-15 | 1979-06-20 | Basf Ag | Removal of phosgene from off-gas |
| CN101018596A (en) * | 2004-09-13 | 2007-08-15 | 巴斯福股份公司 | Method for separating hydrogen chloride and phosgene |
| US20090104099A1 (en) * | 2007-10-17 | 2009-04-23 | Au-Yeung Patrick H | Rich gas absorption apparatus and method |
| CN101348252A (en) * | 2008-04-25 | 2009-01-21 | 甘肃银光化学工业集团有限公司 | Phosgene recovery method for toluene diisocyanate production process |
| CN101348446A (en) * | 2008-04-25 | 2009-01-21 | 甘肃银光化学工业集团有限公司 | Phosgene removing method for TDI production |
| CN101671273A (en) * | 2009-09-18 | 2010-03-17 | 天津大学 | Method for recycling phosgene in continuous production process of toluene di-isocyanate |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105289247A (en) * | 2015-10-20 | 2016-02-03 | 安徽广信农化股份有限公司 | Stearoyl chloride phosgene recovery method |
| CN106008268A (en) * | 2016-05-18 | 2016-10-12 | 江苏蓝丰生物化工股份有限公司 | Method for recycling phosgene in tail gas produced through thermo-optical reaction for synthesis of 3,5-dichlorophenyl isocyanate |
| CN111686556A (en) * | 2020-07-31 | 2020-09-22 | 济宁康盛彩虹生物科技有限公司 | Industrial treatment system and treatment method for solid light tail gas in process of synthesizing fluorinated phase transfer catalyst |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN206103690U (en) | Acyl chlorides chemical industry preface sulfur dioxide exhaust purification recovery unit | |
| CN101104533A (en) | A kind of treatment method of H-acid production wastewater | |
| CN103640111B (en) | A kind of PET bottle sheet cleaning | |
| CN102504902A (en) | Method and device for producing biomass natural gas by separating biogas with high hydrogen sulfide content | |
| CN101367507A (en) | Gas removing, filtering and extracting method for waste sulphuric acid | |
| CN105084369A (en) | Chlorosilane-containing waste gas recovery treatment apparatus | |
| CN102258935A (en) | Recovery and utilization method of phosgene in phosgenation reaction tail gas | |
| CN116422372B (en) | Composite catalyst material based on rapid degradation of microplastic and preparation method and application thereof | |
| CN103253633B (en) | Chlorate electrolysis tail gas recycle hydrogen method | |
| CN103911681B (en) | A kind of method utilizing the PET bottle manufacture weaving long filament of recovery | |
| CN202224050U (en) | Complete equipment for treating tail gas of graphitizing furnace | |
| CN103253716A (en) | New technology of recycling ammonium bicarbonate during production of cobaltosic oxide | |
| CN103550989B (en) | The integrated conduct method of tail gas in a kind of mercury chloride production process | |
| CN214020023U (en) | Preparation facilities of hydrogen chloride methanol solution | |
| CN205035304U (en) | Reduce production system that rubber vulcanization accelerator DPG liquid ammonia consumed | |
| CN102698462A (en) | Acid mist condensing water-saving method of reaction kettle for producing aluminum polychlorid and system thereof | |
| CN103640110B (en) | A kind of PET bottle sheet cleaning energy saving circulating system | |
| CN207546148U (en) | The equipment of monoxone vent gas treatment recovery of acetic acid and hydrochloric acid | |
| CN203030166U (en) | High-purity hydrochloric acid tail gas recycling device | |
| CN206033271U (en) | High -purity poly aluminium chloride production system | |
| CN205109317U (en) | Vacuum tail gas treatment system | |
| BR112014023645B1 (en) | METHOD USING INDUSTRIAL COMBUSTION GAS FOR REMOVAL OF METALLIC IONS FROM RICE SHELLS | |
| CN205387476U (en) | System for hydrogen effectively utilizes in realizing chlor -alkali by -product | |
| CN205913993U (en) | Poly aluminium chloride tail gas processing device | |
| CN203816465U (en) | Waste gas absorption tower |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| DD01 | Delivery of document by public notice |
Addressee: Gu Weiwen Document name: Notification that Application Deemed to be Withdrawn |
|
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20111130 |