CN101429093B - Energy-saving process for producing monochloro methane with liquid phase catalysis method - Google Patents
Energy-saving process for producing monochloro methane with liquid phase catalysis method Download PDFInfo
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- CN101429093B CN101429093B CN2008101595818A CN200810159581A CN101429093B CN 101429093 B CN101429093 B CN 101429093B CN 2008101595818 A CN2008101595818 A CN 2008101595818A CN 200810159581 A CN200810159581 A CN 200810159581A CN 101429093 B CN101429093 B CN 101429093B
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- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical compound ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 title claims abstract description 84
- 239000007791 liquid phase Substances 0.000 title claims abstract description 53
- 238000000034 method Methods 0.000 title claims abstract description 49
- 238000006555 catalytic reaction Methods 0.000 title description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 276
- 238000006243 chemical reaction Methods 0.000 claims abstract description 42
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 32
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims abstract description 30
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims abstract description 30
- 239000012071 phase Substances 0.000 claims abstract description 29
- 238000004519 manufacturing process Methods 0.000 claims abstract description 9
- 238000005660 chlorination reaction Methods 0.000 claims description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 8
- 239000001257 hydrogen Substances 0.000 claims description 8
- 229910052739 hydrogen Inorganic materials 0.000 claims description 8
- 238000002309 gasification Methods 0.000 claims description 5
- 239000002253 acid Substances 0.000 abstract description 18
- 238000001035 drying Methods 0.000 abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 8
- 238000007906 compression Methods 0.000 abstract description 7
- 230000006835 compression Effects 0.000 abstract description 7
- 238000009833 condensation Methods 0.000 abstract description 7
- 230000005494 condensation Effects 0.000 abstract description 7
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 abstract description 6
- 239000003054 catalyst Substances 0.000 abstract description 6
- 239000007788 liquid Substances 0.000 abstract description 6
- 238000005406 washing Methods 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract description 3
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 abstract 2
- 239000000203 mixture Substances 0.000 abstract 1
- 239000000376 reactant Substances 0.000 abstract 1
- 235000005074 zinc chloride Nutrition 0.000 abstract 1
- 239000011592 zinc chloride Substances 0.000 abstract 1
- 238000011084 recovery Methods 0.000 description 14
- 238000004140 cleaning Methods 0.000 description 13
- 239000000047 product Substances 0.000 description 11
- 229940050176 methyl chloride Drugs 0.000 description 9
- 239000003513 alkali Substances 0.000 description 8
- 238000005554 pickling Methods 0.000 description 8
- 239000002351 wastewater Substances 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 230000003197 catalytic effect Effects 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 4
- 239000006200 vaporizer Substances 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000000178 monomer Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000002093 peripheral effect Effects 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 229950005499 carbon tetrachloride Drugs 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- NEHMKBQYUWJMIP-NJFSPNSNSA-N chloro(114C)methane Chemical compound [14CH3]Cl NEHMKBQYUWJMIP-NJFSPNSNSA-N 0.000 description 1
- 229960001701 chloroform Drugs 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000008236 heating water Substances 0.000 description 1
- 239000002917 insecticide Substances 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 150000001282 organosilanes Chemical class 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- VZGDMQKNWNREIO-UHFFFAOYSA-N tetrachloromethane Chemical compound ClC(Cl)(Cl)Cl VZGDMQKNWNREIO-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention relates to an energy-saving production technique for preparing monochloro methane by the liquid-phase method, which comprises the following steps: a zinc chloride solution is taken as catalyst, and hydrogen chloride and methanol react in a reactor to generate the monochloro methane, wherein gas-phase hydrogen chloride enters into the reactor, or the gas-phase hydrogen chloride is mixed with partial gas-phase methanol which is gasified by a methanol gasifier, and the mixture enters into the reactor; partial methanol or all the methanol directly enters into the reactor for reaction in the state of liquid phase; and liquid-phase methanol enters into the reactor when the temperature in the reactor is between 150 and 160 DEG C. After a reactant enters into a vapor-liquid separation tank, liquid phase returns back to the reactor, and gas-phase products are subjected to acid washing, alkaline washing, sulfuric acid drying, compression and condensation and then stored as finished products; and a methanol-bearing diluted hydrochloric acid obtained after acid washing enters into a methanol reclaiming tower for reclaiming unreacted methanol. The energy-saving production technique does not need circulating temperature reduction on the outside of a kettle, saves the electrical energy of a pump and consumption of circulating water, and has obvious energy-saving effect.
Description
Technical field
The present invention relates to produce the preparation method of the main raw material methyl chloride of organosilane monomer, particularly a kind of liquid catalytic prepares the energy-saving processing technique of monochloro methane.
Technical background
Organosilicon macromolecule material development obtains very fast development as the methyl chloride of the main raw material of synthesizing organosilicon monomer rapidly both at home and abroad at present.The method of at present synthetic monochloro methane mainly contains by-product absorption method, methane chlorination method, methyl alcohol hydrochlorinate method.
The by-product absorption method mainly is that insecticide factory reclaims the by product monochloro methane through the simple refining product that obtains.Its advantage is that cost is low.Shortcoming is the requirement that output is little, product purity can't reach synthesizing organosilicon monomer.
The methane chlorination method is meant that with methane and chlorine be raw material, and reaction generates polychloride in the thermal chlorination reactor again, can obtain monochloro methane, methylene dichloride, trichloromethane, tetrachloromethane through rectifying separation.Shortcoming mainly is the complicated energy consumption height of the many separating technologies of product category that obtains.
Methyl alcohol hydrochlorinate method is meant that methyl alcohol and hydrogenchloride are mixed in proportion and enters reactor, and reaction product obtains purified methyl chloride after through washing, alkali cleaning, sulfuric acid drying.Methyl alcohol hydrochlorinate method is divided into gas-phase catalysis, liquid catalytic, liquid phase on-catalytic method.The gas-phase catalysis catalyzer is an activated alumina, and the liquid catalytic catalyzer is a liquor zinci chloridi, and liquid phase on-catalytic method is not used catalyzer.Methyl alcohol hydrochlorinate method reaction principle is as follows:
CH
3OH+HCl＝CH
3Cl+H
20
Because this reaction is a thermopositive reaction, conventional way is at reactor peripheral hardware chuck in the production, feeds the recirculated water cooling in the chuck, or carries out the extracorporeal circulation control reaction temperature at reactor peripheral hardware heating water cooler.Can lose certain heat by heat exchange method like this, the heat that makes reaction produce can not be fully utilized.
Summary of the invention
At the deficiencies in the prior art, the invention provides the energy-saving processing technique that a kind of liquid phase method prepares monochloro methane.
Summary of the invention
The present invention prepares on the basis of monochloro methane technology at existing liquid phase method, change the mode of whole gas-phase feed into the Partial Liquid Phase charging, promptly when charging, feed a certain amount of liquid phase methanol feedstock, utilize the reaction heat of reaction system in reactor, liquid phase methyl alcohol to be gasified, also absorption reaction heat release simultaneously, thereby saved the reactor cooling with the consumption of recirculated water or the power consumption of the dynamo-electric equipment of extracorporeal circulation, reached energy-conservation purpose.
Detailed Description Of The Invention
Technical scheme of the present invention is as follows:
A kind of liquid phase method prepares the energy-saving processing technique of monochloro methane, comprise with the liquor zinci chloridi being catalyzer, hydrogenchloride and methyl alcohol react in reactor, generate monochloro methane, it is characterized in that, gas phase chlorination hydrogen or gas phase chlorination hydrogen and the part gas-phase methanol after methanol gasifying device gasification is mixed into reactor, and partly or entirely methyl alcohol directly enters reactor with liquid phase state and participates in reaction, begins to feed liquid phase methyl alcohol in the reactor temperature 150-160 ℃ the time.
Above reaction product is by behind the vapor-liquid separation tank, and liquid-phase reflux is to reactor, and the gas-phase product monochloro methane stores as finished product behind overpickling, alkali cleaning, sulfuric acid drying, compression condensation.
Above-mentioned to the resulting dilute hydrochloric acid that contains methyl alcohol of gas-phase product monochloro methane pickling, enter Methanol Recovery and hydrogenchloride recovery system again and reclaim unreacted methanol and hydrogenchloride.
Temperature of reaction is 100 ℃-180 ℃ in the reactor, and reaction pressure is 0.06MPa-0.2Mpa.
Preferably, temperature of reaction is 120-160 ℃ in the reactor, and reaction pressure is 0.06MPa-0.18MPa.
The mass ratio that liquid phase methyl alcohol feeds is participated in the 1%-100% of the methanol quality of reaction for all.Preferably, the quality of liquid phase methyl alcohol feeding is participated in the 5%-80% of the methanol quality of reaction for all.Preferred, the quality that liquid phase methyl alcohol feeds is participated in the 20%-60% of the methanol quality of reaction for all.
Preferably, the concentration of catalyst reactor liquor zinci chloridi is 50%-85% mass percent.
The equipment of reaction product aftertreatment is same as the prior art.
Compared with prior art, excellent results of the present invention is as follows:
1, participate in reaction because part methyl alcohol need not directly enter reactor through gasifier, so energy-saving effect is obvious.
2, because the method for control reaction temperature is to feed liquid phase methyl alcohol, therefore can avoid reactor to produce suddenly cold and hot phenomenon, extension reactor life-span.
3, save the pump electric energy owing to need not carry out still outer circulation cooling, saving recirculated water consumption effect is obvious.
4, reaction product acid waste water after overpickling goes Methanol Recovery and hydrogenchloride recovery system to reclaim hydrogenchloride and methyl alcohol, so methyl alcohol and hydrogenchloride consumes lowly, and the sewage qualified discharge does not produce acid waste water.
Description of drawings
Fig. 1 is a process flow sheet of the present invention.Wherein 1 is the methyl alcohol vaporizer, 2 is reactor, and 3 for the pickling tower, and 4 comprise alkali cleaning, drying, compression, condensation for after-treatment system, 5 is Methanol Recovery and hydrogenchloride recovery system, 6 is liquid phase methyl alcohol, and 7 is gas-phase methanol, the 8 thick methyl chloride for the reactor reaction generation, 8 ' for treating the thick methyl chloride of alkali cleaning after the pickling, 9 acid waste waters that in acid cleaning process, produce for the pickling tower, 10 is the finished product methyl chloride, 11 is hydrogenchloride.
Embodiment
Following examples are to further specify of the present invention, but the present invention is not limited to this.
Embodiment 1:
A kind of liquid phase method prepares the energy-saving processing technique of monochloro methane, with the liquor zinci chloridi is catalyzer, hydrogenchloride and methyl alcohol react in reactor, generate monochloro methane, wherein, the concentration of catalyst reactor liquor zinci chloridi is 60%-65% mass percent, gas phase chlorination hydrogen and the part gas-phase methanol after the gasification of methanol gasifying device is mixed into reactor, another part methyl alcohol directly enters reactor with liquid phase state and participates in reaction, and the mass ratio that liquid phase methyl alcohol feeds is participated in 40% of the methanol quality that reacts for all.
Technical process as shown in Figure 1, Partial Liquid Phase methyl alcohol 6 enters methyl alcohol vaporizer 1 and is vaporizated into gas-phase methanol 7, gas-phase methanol 7 with enter reactor 2 after hydrogenchloride 11 mixes, controlling reactor 2 reaction pressures begin to feed liquid phase methyl alcohol 6 at 0.06MPa when temperature reaches 155 ℃ of temperature of reaction in the question response device 2.The thick monochloro methane 8 that does not purify that reaction produces in the reactor 2 enters after-treatment system 4 after 3 pickling of overpickling tower carries out alkali cleaning, drying, compression, condensation again and produces finished product liquid phase methyl chloride 10.The acid waste water 9 that acid water wash column 3 produces in acid cleaning process enters Methanol Recovery and hydrogenchloride recovery system 5 reclaims methyl alcohol 6 and hydrogenchloride 11.
Embodiment 2:
A kind of liquid phase method prepares the energy-saving processing technique of monochloro methane, with the liquor zinci chloridi is catalyzer, hydrogenchloride and methyl alcohol react in reactor, generate monochloro methane, wherein, the concentration of catalyst reactor liquor zinci chloridi is 60%-65% mass percent, gas phase chlorination hydrogen and the part gas-phase methanol after the gasification of methanol gasifying device is mixed into reactor, another part methyl alcohol directly enters reactor with liquid phase state and participates in reaction, and the mass ratio that liquid phase methyl alcohol feeds is participated in 80% of the methanol quality that reacts for all.
Technical process as shown in Figure 1, Partial Liquid Phase methyl alcohol 6 enters methyl alcohol vaporizer 1 and is vaporizated into gas-phase methanol 7, gas-phase methanol 7 with enter reactor 2 after hydrogenchloride 11 mixes, controlling reactor 2 reaction pressures begin to feed liquid phase methyl alcohol 6 when temperature reaches 158 ℃ of temperature of reaction in the question response device 2 between 0.1MPa.The thick monochloro methane 8 that does not purify that reaction produces in the reactor 2 enters after-treatment system 4 after 3 pickling of overpickling tower carries out alkali cleaning, drying, compression, condensation again and produces finished product liquid phase methyl chloride 10.The acid waste water 9 that acid water wash column 3 produces in acid cleaning process enters Methanol Recovery and hydrogenchloride recovery system 5 reclaims methyl alcohol 6 and hydrogenchloride 11.
Embodiment 3:
A kind of liquid phase method prepares the energy-saving processing technique of monochloro methane, with the liquor zinci chloridi is catalyzer, hydrogenchloride and methyl alcohol react in reactor, generate monochloro methane, wherein, the concentration of catalyst reactor liquor zinci chloridi is 60%-65% mass percent, gas phase chlorination hydrogen and the part gas-phase methanol after the gasification of methanol gasifying device is mixed into reactor, another part methyl alcohol directly enters reactor with liquid phase state and participates in reaction, and the mass ratio that liquid phase methyl alcohol feeds is participated in 20% of the methanol quality that reacts for all.
Technical process as shown in Figure 1, Partial Liquid Phase methyl alcohol 6 enters methyl alcohol vaporizer 1 and is vaporizated into gas-phase methanol 7, gas-phase methanol 7 with enter reactor 2 after hydrogenchloride 11 mixes, controlling reactor 2 reaction pressures begin to feed liquid phase methyl alcohol 6 at 0.18MPa when temperature reaches 160 ℃ of temperature of reaction in the question response device 2.The thick monochloro methane 8 that does not purify that reaction produces in the reactor 2 enters after-treatment system 4 after 3 pickling of overpickling tower carries out alkali cleaning, drying, compression, condensation again and produces finished product liquid phase methyl chloride 10.The acid waste water 9 that acid water wash column 3 produces in acid cleaning process enters Methanol Recovery and hydrogenchloride recovery system 5 reclaims methyl alcohol 6 and hydrogenchloride 11.
Embodiment 4:
A kind of liquid phase method prepares the energy-saving processing technique of monochloro methane, with the liquor zinci chloridi is catalyzer, hydrogenchloride and methyl alcohol react in reactor, generate monochloro methane, wherein, the concentration of catalyst reactor liquor zinci chloridi is 65% mass percent, and gas phase chlorination hydrogen and liquid phase methanol mixed enter reactor.
Technical process as shown in Figure 1, liquid phase methyl alcohol 6 with enter reactor 2 after hydrogenchloride 11 mixes, controlling reactor 2 reaction pressures are at 0.2MPa, temperature reaches 160 ℃ of temperature of reaction in the controlling reactor 2.The thick monochloro methane 8 that does not purify that reaction produces in the reactor 2 enters after-treatment system 4 after 3 pickling of overpickling tower carries out alkali cleaning, drying, compression, condensation again and produces finished product liquid phase methyl chloride 10.The acid waste water 9 that acid water wash column 3 produces in acid cleaning process enters Methanol Recovery and hydrogenchloride recovery system 5 reclaims methyl alcohol 6 and hydrogenchloride 11.
Claims (6)
1. a liquid phase method prepares the energy-saving production method of monochloro methane, comprise with the liquor zinci chloridi being catalyzer, hydrogenchloride and methyl alcohol react in reactor, generate monochloro methane, it is characterized in that, gas phase chlorination hydrogen or gas phase chlorination hydrogen and the part gas-phase methanol after methanol gasifying device gasification is mixed into reactor, and part methyl alcohol directly enters reactor with liquid phase state and participates in reaction, begins to feed liquid phase methyl alcohol in the reactor temperature 150-160 ℃ the time.
2. liquid phase method as claimed in claim 1 prepares the energy-saving production method of monochloro methane, it is characterized in that, temperature of reaction is 100 ℃-180 ℃ in the reactor, and reaction pressure is 0.06MPa-0.2MPa.
3. liquid phase method as claimed in claim 1 prepares the energy-saving production method of monochloro methane, it is characterized in that, temperature of reaction is 120-160 ℃ in the reactor, and reaction pressure is 0.06MPa-0.18MPa.
4. liquid phase method as claimed in claim 1 prepares the energy-saving production method of monochloro methane, it is characterized in that, the quality that liquid phase methyl alcohol feeds is participated in the 5%-80% of the methanol quality of reaction for all.
5. liquid phase method as claimed in claim 1 prepares the energy-saving production method of monochloro methane, it is characterized in that, the quality that liquid phase methyl alcohol feeds is participated in the 20%-60% of the methanol quality of reaction for all.
6. liquid phase method as claimed in claim 1 prepares the energy-saving production method of monochloro methane, it is characterized in that, the concentration of the liquor zinci chloridi in the reactor is the 50%-85% mass percent.
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| CN2008101595818A CN101429093B (en) | 2008-11-28 | 2008-11-28 | Energy-saving process for producing monochloro methane with liquid phase catalysis method |
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| CN2008101595818A CN101429093B (en) | 2008-11-28 | 2008-11-28 | Energy-saving process for producing monochloro methane with liquid phase catalysis method |
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| CN101429093B true CN101429093B (en) | 2011-11-09 |
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Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102295517A (en) * | 2011-07-05 | 2011-12-28 | 镇江市东煌化工有限公司 | Process of synthesizing methyl chloride with hydrogen chloride gas by-produced in production of phosphorous acid from phosphorus trichloride |
| CN102408300B (en) * | 2011-11-11 | 2014-01-08 | 河北科技大学 | Method for preparing chloromethane and ammonia by liquid phase method |
| CN102718623A (en) * | 2012-07-13 | 2012-10-10 | 自贡鸿鹤化工股份有限公司 | Method of producing methane chloride by using byproduct hydrogen chloride of tetrachloroethylene device |
| CN102850178A (en) * | 2012-08-24 | 2013-01-02 | 江苏振方医药化工有限公司 | Method for synthesizing ethyl chloride by using gas phase hydrogen chloride and ethanol |
| CN103922547B (en) * | 2014-04-30 | 2015-03-25 | 南通江天化学品有限公司 | Flow distribution treatment process for byproduct of methanol-containing hydrochloric acid during chloromethane synthesis |
| CN105985217B (en) * | 2015-02-04 | 2018-11-02 | 山东东岳有机硅材料股份有限公司 | Reaction system and its application of reactant utilization rate are improved in a kind of production of chloromethanes |
| CN106008151A (en) * | 2016-07-22 | 2016-10-12 | 合盛硅业股份有限公司 | Methyl chloride synthesis method |
| CN108409526B (en) * | 2018-03-09 | 2020-11-20 | 中国化学赛鼎宁波工程有限公司 | Methane chloride energy-saving production system and method |
| CN112898115B (en) * | 2018-06-28 | 2022-05-31 | 湖北兴瑞硅材料有限公司 | Process for synthesizing chloromethane from hydrogen chloride under pressure |
| CN113548941A (en) * | 2020-04-24 | 2021-10-26 | 蓝星（北京）技术中心有限公司 | Synthesis method and device of methane chloride |
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Owner name: BEIJING PETROCHEMICAL INDUSTRY DESIGN RESEARCH INS Free format text: FORMER OWNER: SHANDONG DONGYUE SILICONE MATERIALS CO., LTD. Effective date: 20100401 Owner name: SHANDONG DONGYUE SILICONE MATERIALS CO., LTD. |
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Inventor after: Meng Xiangfeng Inventor after: Liu Yingchun Inventor after: Wang Weidong Inventor after: Yi Gang Inventor after: Liu Qiang Inventor before: Wang Weidong Inventor before: Yi Gang Inventor before: Liu Qiang |
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Free format text: CORRECT: ADDRESS; FROM: 256401 TANGSHAN TOWN, HUANTAI COUNTY, SHANDONG PROVINCE TO: 100011 AUXILIARY BUILDING, NO.56, ANWAI AVENUE, DONGCHENG DISTRICT, BEIJING CITY Free format text: CORRECT: INVENTOR; FROM: WANG WEIDONG YI GANG LIU QIANG TO: MENG XIANGFENG LIU YINGCHUN WANG WEIDONG YI GANG LIU QIANG |
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Effective date of registration: 20100401 Address after: 100011 Beijing city Dongcheng District An Wai Avenue No. 56 auxiliary building Applicant after: Shandong Dongyue Silicon Material Co., Ltd. Co-applicant after: Shandong Dongyue Silicon Material co., Ltd. Address before: 256401 Tangshan Town, Huantai County, Shandong Province Applicant before: Shandong Dongyue Silicon Material co., Ltd. |
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Address after: 100020 Beijing city Chaoyang District Tian Yuan Garden No. 7, 3 floor 301 Co-patentee after: Shandong Dongyue organosilicon material Limited by Share Ltd Patentee after: Beijing Petrochemical Engineering Co., Ltd. Address before: 100011 auxiliary building, No. 56 An Wai Street, Dongcheng District, Beijing Co-patentee before: Shandong Dongyue Silicon Material co., Ltd. Patentee before: Shandong Dongyue Silicon Material Co., Ltd. |
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