CN203955191U - Polymeric kettle feeding device - Google Patents
Polymeric kettle feeding device Download PDFInfo
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- CN203955191U CN203955191U CN201420278340.6U CN201420278340U CN203955191U CN 203955191 U CN203955191 U CN 203955191U CN 201420278340 U CN201420278340 U CN 201420278340U CN 203955191 U CN203955191 U CN 203955191U
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- polymeric kettle
- pipeline
- coil pipe
- deionized water
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Abstract
The utility model relates to polyvinyl-chloride use polymeric kettle technical field, is a kind of polymeric kettle feeding device; This polymeric kettle feeding device comprises polymeric kettle and base; Polymeric kettle is fixedly mounted on base, on the top of polymeric kettle, be respectively arranged with the first feed end and the second feed end, on the first feed end, be fixedly connected with monomer line, on the second feed end, be fixedly connected with terminator pipeline, bottom at polymeric kettle is provided with discharge end, is fixedly connected with discharging pipeline on discharge end.In the utility model, VCM, cold deionized water, aqueous dispersant and aqueous solution of buffer agent add simultaneously, not only saved the pan feeding time, also avoided the generation of polychloroethylene with high polymerization degree resin when lower temperature in polymeric kettle pan feeding process, reduced Corvic molecular weight distribution width, the Corvic performance that the utility model is obtained is more stable, save cost, improved production efficiency.
Description
Technical field
the utility model relates to polyvinyl-chloride use polymeric kettle technical field, is a kind of polymeric kettle feeding device.
Background technology
produce at present the 110m of polyvinyl chloride
3
the cold deionized water of polymeric kettle pan feeding process using, hot deionized water intersection enter material way, its specific embodiment is: after polymeric kettle is coated with still operation, play cold deionized water operation, start and coldly without ionic pump, cold deionized water is added polymeric kettle from still bottom after by mass flowmenter, start buffer charge pump, dispersant charge pump, initator charge pump simultaneously buffer, dispersant, initator are added in cold deionized water pipeline, buffer, dispersant, initator are brought polymeric kettle into by cold deionized water.After the auxiliary agents such as buffer, dispersant and initator have added prior to cold deionized water, after cold deionized water has added, start monomer pan feeding pump and add respectively recovery monomer and fresh monomer, finally start hot deionized water pump and add 120 ℃ of overheated deionized waters in polymeric kettle, hot deionized water has added rear polymerization temperature in the kettle to approach reaction temperature (setting reaction temperature T ± 2 ℃), start constant temperature polymerisation, whole polymerization pan feeding process is consuming time at 65 minutes.
but there is following problem in existing technique: (1) existing pan feeding technique, according to hot deionized water, cold deionized water temperature computation addition, is added in polymeric kettle by DCS control system automatic gauge, and this pan feeding technique pan feeding time is longer, and the utilization rate of polymeric kettle is lower; (2) polymerization temperature is almost the unique factor that determines Corvic molecular weight, and in polymerization is produced, Corvic molecular weight represents with viscosity number, Bing Yong viscosity number district Corvic model.In above pan feeding technique, initator enters in polymeric kettle by cold deionized water, after cold water pan feeding completes, VCM adds in polymeric kettle, now polymeric kettle temperature does not reach setting reaction temperature, existence due to initator, VCM starts to carry out polymerisation under the condition lower than setting reaction temperature, until hot deionized water pan feeding could carry out polymerisation after completing in setting range of reaction temperature, during this, the reaction of part VCM generates the Corvic of higher viscosity number, cause Corvic product molecular weight distribution width to increase, the processing characteristics of Corvic and the bad stability of goods.
Summary of the invention
the utility model provides a kind of polymeric kettle feeding device, has overcome the deficiency of above-mentioned prior art, and it can effectively solve the 110m of existing production polyvinyl chloride
3
polymeric kettle pan feeding technique exists the pan feeding time to grow, polymeric kettle utilization rate is low, the problem of the poor stability of product Corvic.
the technical solution of the utility model realizes by following measures: a kind of polymeric kettle feeding device, comprises polymeric kettle and base, polymeric kettle is fixedly mounted on base, on the top of polymeric kettle, be respectively arranged with the first feed end and the second feed end, on the first feed end, be fixedly connected with monomer line, on the second feed end, be fixedly connected with terminator pipeline, bottom at polymeric kettle is provided with discharge end, on discharge end, be fixedly connected with discharging pipeline, on discharging pipeline, be installed with the first control valve, on the discharging pipeline between polymeric kettle and the first control valve, be installed with threeway, in threeway, be fixedly connected with hot deionized water pipeline, on hot deionized water pipeline, be installed with the second control valve, on the hot deionized water pipeline between threeway and the second control valve, be fixedly connected with respectively initator pipeline and cold deionized water pipeline, on cold deionized water pipeline, be installed with the 3rd control valve, on the cold deionized water pipeline between hot deionized water pipeline and the 3rd control valve, be fixedly connected with respectively dispersant pipeline and buffer pipeline, in monomer line, terminator pipeline, initator pipeline, on dispersant pipeline and buffer pipeline, be installed with respectively valve.
the further optimization and/or improvements to above-mentioned utility model technical scheme below:
above-mentionedly on monomer line, terminator pipeline, initator pipeline, dispersant pipeline, buffer pipeline, hot deionized water pipeline and cold deionized water pipeline, be installed with respectively mass flowmenter.
the above-mentioned check-valves that is installed with in monomer line.
above-mentionedly in polymeric kettle bottom, be installed with agitator, the stirring end of agitator is positioned at polymeric kettle.
the above-mentioned inner coil pipe that is installed with vertical direction in the cavity of polymeric kettle, the liquid feeding end of inner coil pipe is positioned at outside the bottom of polymeric kettle, the outlet end of inner coil pipe is positioned at outside the top of polymeric kettle, on the outer wall of polymeric kettle, be fixedly connected with the outer coil pipe of horizontal direction, the liquid feeding end of outer coil pipe and the outlet end of inner coil pipe are fixed together; Or/and polymeric kettle is 110M
3
polymeric kettle.
in the utility model, VCM, cold deionized water, aqueous dispersant and aqueous solution of buffer agent add simultaneously, not only saved the pan feeding time, also avoided the generation of polychloroethylene with high polymerization degree resin when lower temperature in polymeric kettle pan feeding process, reduced Corvic molecular weight distribution width, the Corvic performance that the utility model is obtained is more stable, save cost, improved production efficiency.
Accompanying drawing explanation
accompanying drawing 1 is process flow diagram of the present utility model.
coding in accompanying drawing is respectively: 1 is polymeric kettle, and 2 is base, and 3 is monomer line, 4 is terminator pipeline, and 5 is discharging pipeline, and 6 is the first control valve, 7 is threeway, and 8 is hot deionized water pipeline, and 9 is the second control valve, 10 is initator pipeline, and 11 is cold deionized water pipeline, and 12 is the 3rd control valve, 13 is dispersant pipeline, and 14 is buffer pipeline, and 15 is check-valves, 16 is agitator, and 17 is inner coil pipe, and 18 is outer coil pipe.
The specific embodiment
the utility model is not subject to the restriction of following embodiment, can determine concrete embodiment according to the technical solution of the utility model and actual conditions.
in the utility model, for convenience of description, the description of the relative position relation of each parts is to be all described according to the Butut mode of Figure of description 1, as: the position relationship of forward and backward, upper and lower, left and right etc. is to determine according to the Butut direction of Figure of description 1.
below in conjunction with embodiment and accompanying drawing, the utility model is further described:
embodiment 1, and as shown in Figure 1, this polymeric kettle feeding device comprises polymeric kettle 1 and base 2, polymeric kettle 1 is fixedly mounted on base 2, on the top of polymeric kettle 1, be respectively arranged with the first feed end and the second feed end, on the first feed end, be fixedly connected with monomer line 3, on the second feed end, be fixedly connected with terminator pipeline 4, bottom at polymeric kettle 1 is provided with discharge end, on discharge end, be fixedly connected with discharging pipeline 5, on discharging pipeline 5, be installed with the first control valve 6, on the discharging pipeline 5 between polymeric kettle 1 and the first control valve 6, be installed with threeway 7, in threeway 7, be fixedly connected with hot deionized water pipeline 8, on hot deionized water pipeline 8, be installed with the second control valve 9, on the hot deionized water pipeline 8 between threeway 7 and the second control valve 9, be fixedly connected with respectively initator pipeline 10 and cold deionized water pipeline 11, on cold deionized water pipeline 11, be installed with the 3rd control valve 12, on the cold deionized water pipeline 11 between hot deionized water pipeline 8 and the 3rd control valve 12, be fixedly connected with respectively dispersant pipeline 13 and buffer pipeline 14, in monomer line 3, terminator pipeline 4, initator pipeline 10, on dispersant pipeline 13 and buffer pipeline 14, be installed with respectively valve.Like this, the first control valve 6 is convenient to control discharging; The second control valve 9 is convenient to control the addition of hot deionized water; The 3rd control valve 12 is convenient to control the addition of cold deionized water.
can according to actual needs, above-described embodiment 1 be made further optimization and/or improvements:
as required, on monomer line 3, terminator pipeline 4, initator pipeline 10, dispersant pipeline 13, buffer pipeline 14, hot deionized water pipeline 8 and cold deionized water pipeline 11, be installed with respectively mass flowmenter.Like this, mass flowmenter is convenient to control the quality that enters polymeric kettle 1 material in each pipeline.
as shown in Figure 1, in monomer line 3, be installed with check-valves 15.Like this, check-valves 15 prevents that VCM from flowing backwards.
as shown in Figure 1, in polymeric kettle 1 bottom, be installed with agitator 16, the stirring end of agitator 16 is positioned at polymeric kettle 1.Like this, agitator 16 is convenient to stir, and the material in polymeric kettle 1 is evenly mixed.
as shown in Figure 1, in the cavity of polymeric kettle 1, be installed with the inner coil pipe 17 of vertical direction, the liquid feeding end of inner coil pipe 17 is positioned at outside the bottom of polymeric kettle 1, the outlet end of inner coil pipe 17 is positioned at outside the top of polymeric kettle 1, on the outer wall of polymeric kettle 1, be fixedly connected with the outer coil pipe 18 of horizontal direction, the outlet end of the liquid feeding end of outer coil pipe 18 and inner coil pipe 17 is fixed together; Or/and polymeric kettle 1 is 110M
3
polymeric kettle.Like this, during work, outwards in coil pipe 18 and inner coil pipe 17, pass into recirculated water, be convenient to control polymeric kettle 1 reaction temperature.
as shown in Figure 1, the using method of above-described embodiment polymeric kettle feeding device is carried out in the steps below: the first step, on the inwall of polymeric kettle, smear anti-fouling agent, control polymeric kettle internal pressure and be-0.07Mpa extremely-0.05Mpa, second step, by cold deionized water pipeline, in polymeric kettle, add 190 parts to 200 parts cold deionized waters by weight, by dispersant pipeline, in polymeric kettle, add 8.75 parts of aqueous dispersants that are 4% to 10.5 parts of mass percent concentrations by weight, by buffer pipeline, in polymeric kettle, add 1 part of aqueous solution of buffer agent that is 10% to 1.5 parts of mass percent concentrations by weight, make cold deionized water carry aqueous dispersant enters in polymeric kettle together with aqueous solution of buffer agent, by monomer line, in polymeric kettle, add 410 parts to 420 parts VCMs and stir by weight simultaneously, the 3rd step after aqueous dispersant, aqueous solution of buffer agent, cold deionized water and VCM pan feeding complete, is added 210 parts of hot deionized waters and stirs by weight by hot deionized water pipeline in polymeric kettle, the 4th step, after hot deionized water pan feeding completes by initator pipeline by weight to adding 0.4 part in polymeric kettle to 0.45 part of mass percent concentration initiator solution that is 50% and stirring, at pressure, be that 0.82Mpa to 0.83Mpa, temperature are to react 260min to 270min at 56.5 ℃ to 57.5 ℃, after reaction, by terminator pipeline, obtain Corvic by weight to adding 0.25 part to 0.35 part terminator and stir in polymeric kettle, Corvic is discharged by discharging pipeline.
as shown in Figure 1, the using method of above-described embodiment polymeric kettle feeding device is carried out in the steps below: the first step, on the inwall of polymeric kettle, smear anti-fouling agent, control polymeric kettle internal pressure and be-0.07Mpa or-0.05Mpa, second step, by cold deionized water pipeline, in polymeric kettle, add 190 parts or 200 parts of cold deionized waters by weight, by dispersant pipeline, in polymeric kettle, add 8.75 parts or 10.5 parts of aqueous dispersants that mass percent concentration is 4% by weight, by buffer pipeline, in polymeric kettle, add 1 part or 1.5 parts of aqueous solution of buffer agent that mass percent concentration is 10% by weight, make cold deionized water carry aqueous dispersant enters in polymeric kettle together with aqueous solution of buffer agent, simultaneously by monomer line by weight to adding 410 parts or 420 parts of VCMs in polymeric kettle and stirring, the 3rd step after aqueous dispersant, aqueous solution of buffer agent, cold deionized water and VCM pan feeding complete, is added 210 parts of hot deionized waters and stirs by weight by hot deionized water pipeline in polymeric kettle, the 4th step, after hot deionized water pan feeding completes by initator pipeline by weight to adding the initiator solution that 0.4 part or 0.45 part of mass percent concentration are 50% in polymeric kettle and stirring, at pressure, be that 0.82Mpa or 0.83Mpa, temperature are at 56.5 ℃ or 57.5 ℃, to react 260min or 270min, after reaction, by terminator pipeline, obtain Corvic by weight to adding 0.25 part or 0.35 part of terminator in polymeric kettle and stirring, Corvic is discharged by discharging pipeline.
can according to actual needs, above-mentioned using method be made further optimization and/or improvements:
as shown in Figure 1, the using method of above-described embodiment polymeric kettle feeding device is carried out in the steps below: the first step, on the inwall of polymeric kettle 1, smear anti-fouling agent, control polymeric kettle 1 internal pressure and be-0.07Mpa extremely-0.05Mpa, second step, by cold deionized water pipeline 11, in polymeric kettle 1, add 19 tons to 20 tons cold deionized waters, by dispersant pipeline 13, in polymeric kettle 1, add 875 kilograms of aqueous dispersants that are 4% to 1050 kilogram-mass percent concentrations, by buffer pipeline 14, in polymeric kettle 1, add the aqueous solution of buffer agent that double centner to 150 kilogram-mass percent concentration is 10%, make cold deionized water carry aqueous dispersant enters in polymeric kettle 1 together with aqueous solution of buffer agent, by monomer line 3, in polymeric kettle 1, add 41 tons to 42 tons VCMs and stir simultaneously, the 3rd step, after aqueous dispersant, aqueous solution of buffer agent, cold deionized water and VCM pan feeding complete, is added 21 tons of hot deionized waters and stirs in polymeric kettle 1 by hot deionized water pipeline 8, the 4th step, after hot deionized water pan feeding completes by initator pipeline 10 to adding 40 kilograms in polymeric kettle 1 to the 45 kilogram-mass percent concentrations initiator solution that is 50% and stirring, at pressure, be that 0.82Mpa to 0.83Mpa, temperature are to react 260min to 270min at 56.5 ℃ to 57.5 ℃, after reaction, by terminator pipeline 4, to adding 25 kilograms to 35 kilograms terminators and stir in polymeric kettle 1, obtain Corvic, Corvic is discharged by discharging pipeline 5.Initator has added rear polymeric kettle 1 temperature to approach or has reached polymeric kettle 1 reaction design temperature, starts polymerisation.The Corvic obtaining is SG-5 type resin; Anti-fouling agent is smeared 10 kilograms to 15 kilograms at every turn; Terminator is existing public reagent.
as shown in Figure 1, the using method of above-described embodiment polymeric kettle feeding device, carry out in the steps below: the first step, on the inwall of polymeric kettle 1, smear anti-fouling agent, control polymeric kettle 1 internal pressure and be-0.07Mpa or-0.05Mpa, second step, by cold deionized water pipeline 11, in polymeric kettle 1, add 19 tons or 20 tons of cold deionized waters, by dispersant pipeline 13 to adding the aqueous dispersant that 875 kilograms or 1050 kilogram-mass percent concentrations are 4% in polymeric kettle 1, by buffer pipeline 14, in polymeric kettle 1, add the aqueous solution of buffer agent that double centner or 150 kilogram-mass percent concentrations are 10%, make cold deionized water carry aqueous dispersant enters in polymeric kettle 1 together with aqueous solution of buffer agent, simultaneously by monomer line 3 to adding 41 tons or 42 tons of VCMs in polymeric kettle 1 and stirring, the 3rd step, after aqueous dispersant, aqueous solution of buffer agent, cold deionized water and VCM pan feeding complete, is added 21 tons of hot deionized waters and stirs in polymeric kettle 1 by hot deionized water pipeline 8, the 4th step, after hot deionized water pan feeding completes by initator pipeline 10 to adding the initiator solution that 40 kilograms or 45 kilogram-mass percent concentrations are 50% in polymeric kettle 1 and stirring, at pressure, be that 0.82Mpa or 0.83Mpa, temperature are at 56.5 ℃ or 57.5 ℃, to react 260min or 270min, after reaction, by terminator pipeline 4, to adding 25 kilograms or 35 kilograms of terminators in polymeric kettle 1 and stirring, obtain Corvic, Corvic is discharged by discharging pipeline 5.
as required, the temperature of cold deionized water is 20 ℃ to 25 ℃; Or/and the temperature of hot deionized water is 110 ℃ to 120 ℃.
as required, anti-fouling agent is polyhydric phenols copolymer; Aqueous dispersant is polyvinyl alcohol water solution; Aqueous solution of buffer agent is ammonium bicarbonate aqueous solution; Initiator solution is the new certain herbaceous plants with big flowers acid isopropyl phenyl ester of peroxidating and the two aqueous solution being configured to for 3:1 by volume of peroxy dicarbonate.
as required, stir speed (S.S.) is 124 revs/min to 126 revs/min; Or/and polymeric kettle 1 is 110M
3
polymeric kettle.
the average behavior parameter of the Corvic obtaining according to the utility model above-described embodiment and the Corvic of existing explained hereafter is shown in Table 1.
the average viscosity of the Corvic that as can be seen from Table 1, the utility model above-described embodiment obtains, average impurity grain number, average volatile content, average apparent density, average flake, 100g resin plasticizer average absorption amount, average whiteness and the mean molecule quantity dispersion of distribution are respectively 111 ml/g, 6,0.12%, 0.52g/ml, 10,24g, 85% and 2.003, and the average viscosity of the Corvic of existing explained hereafter, average impurity grain number, average volatile content, average apparent density, average flake, 100g resin plasticizer average absorption amount, average whiteness and the mean molecule quantity dispersion of distribution are respectively 111 ml/g, 6,0.15%, 0.52g/ml, 14,24g, 85% and 2.105, the average viscosity of the Corvic that the utility model above-described embodiment obtains, average impurity grain number, average apparent density, average flake, the average viscosity of the Corvic of 100g resin plasticizer average absorption amount and average whiteness and existing explained hereafter, average impurity grain number, average apparent density, average flake, 100g resin plasticizer average absorption amount is consistent with average whiteness, but average volatile content and the mean molecule quantity dispersion of distribution of the Corvic of the average volatile content of the Corvic that the utility model above-described embodiment obtains and the more existing explained hereafter of the mean molecule quantity dispersion of distribution are all low, illustrate that the Corvic that Corvic that the utility model obtains produces compared with prior art is more stable, performance is better, and the Corvic that the utility model obtains has reached GB top grade product standard.
in the utility model, VCM, cold deionized water, dispersant and buffer add simultaneously, not only saved the pan feeding time, also avoided the generation of polychloroethylene with high polymerization degree resin when lower temperature in polymeric kettle 1 pan feeding process, reduced Corvic molecular weight distribution width, the Corvic performance that the utility model is obtained is more stable; The utility model pan feeding time has shortened 5 minutes/still compared with prior art pan feeding time average, with single still production capacity 35t, polymeric kettle 1 stirring motor power 312kw, calculate, resin economize on electricity 1.276KW*h per ton, to produce 400,000 tons/year of calculating of resin, 51.04 ten thousand KW*h can economize on electricity the whole year, thereby saved cost, improved production efficiency.
above technical characterictic has formed embodiment of the present utility model, and it has stronger adaptability and implementation result, can increase and decrease according to actual needs non-essential technical characterictic, meets the demand of different situations.
Claims (9)
1. a polymeric kettle feeding device, is characterized in that comprising polymeric kettle and base, polymeric kettle is fixedly mounted on base, on the top of polymeric kettle, be respectively arranged with the first feed end and the second feed end, on the first feed end, be fixedly connected with monomer line, on the second feed end, be fixedly connected with terminator pipeline, bottom at polymeric kettle is provided with discharge end, on discharge end, be fixedly connected with discharging pipeline, on discharging pipeline, be installed with the first control valve, on the discharging pipeline between polymeric kettle and the first control valve, be installed with threeway, in threeway, be fixedly connected with hot deionized water pipeline, on hot deionized water pipeline, be installed with the second control valve, on the hot deionized water pipeline between threeway and the second control valve, be fixedly connected with respectively initator pipeline and cold deionized water pipeline, on cold deionized water pipeline, be installed with the 3rd control valve, on the cold deionized water pipeline between hot deionized water pipeline and the 3rd control valve, be fixedly connected with respectively dispersant pipeline and buffer pipeline, in monomer line, terminator pipeline, initator pipeline, on dispersant pipeline and buffer pipeline, be installed with respectively valve.
2. polymeric kettle feeding device according to claim 1, is characterized in that being installed with respectively mass flowmenter on monomer line, terminator pipeline, initator pipeline, dispersant pipeline, buffer pipeline, hot deionized water pipeline and cold deionized water pipeline.
3. polymeric kettle feeding device according to claim 1 and 2, is characterized in that being installed with in monomer line check-valves.
4. polymeric kettle feeding device according to claim 1 and 2, is characterized in that polymeric kettle bottom is installed with agitator, and the stirring end of agitator is positioned at polymeric kettle.
5. polymeric kettle feeding device according to claim 3, is characterized in that polymeric kettle bottom is installed with agitator, and the stirring end of agitator is positioned at polymeric kettle.
6. polymeric kettle feeding device according to claim 1 and 2, it is characterized in that being installed with in the cavity of polymeric kettle the inner coil pipe of vertical direction, the liquid feeding end of inner coil pipe is positioned at outside the bottom of polymeric kettle, the outlet end of inner coil pipe is positioned at outside the top of polymeric kettle, on the outer wall of polymeric kettle, be fixedly connected with the outer coil pipe of horizontal direction, the liquid feeding end of outer coil pipe and the outlet end of inner coil pipe are fixed together; Or/and polymeric kettle is 110M
3polymeric kettle.
7. polymeric kettle feeding device according to claim 3, it is characterized in that being installed with in the cavity of polymeric kettle the inner coil pipe of vertical direction, the liquid feeding end of inner coil pipe is positioned at outside the bottom of polymeric kettle, the outlet end of inner coil pipe is positioned at outside the top of polymeric kettle, on the outer wall of polymeric kettle, be fixedly connected with the outer coil pipe of horizontal direction, the liquid feeding end of outer coil pipe and the outlet end of inner coil pipe are fixed together; Or/and polymeric kettle is 110M
3polymeric kettle.
8. polymeric kettle feeding device according to claim 4, it is characterized in that being installed with in the cavity of polymeric kettle the inner coil pipe of vertical direction, the liquid feeding end of inner coil pipe is positioned at outside the bottom of polymeric kettle, the outlet end of inner coil pipe is positioned at outside the top of polymeric kettle, on the outer wall of polymeric kettle, be fixedly connected with the outer coil pipe of horizontal direction, the liquid feeding end of outer coil pipe and the outlet end of inner coil pipe are fixed together; Or/and polymeric kettle is 110M
3polymeric kettle.
9. polymeric kettle feeding device according to claim 5, it is characterized in that being installed with in the cavity of polymeric kettle the inner coil pipe of vertical direction, the liquid feeding end of inner coil pipe is positioned at outside the bottom of polymeric kettle, the outlet end of inner coil pipe is positioned at outside the top of polymeric kettle, on the outer wall of polymeric kettle, be fixedly connected with the outer coil pipe of horizontal direction, the liquid feeding end of outer coil pipe and the outlet end of inner coil pipe are fixed together; Or/and polymeric kettle is 110M
3polymeric kettle.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109908851A (en) * | 2017-12-12 | 2019-06-21 | 巴斯夫新材料有限公司 | Polymer reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109908851A (en) * | 2017-12-12 | 2019-06-21 | 巴斯夫新材料有限公司 | Polymer reactor |
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Owner name: XINJIANG HUATAI HEAVY CHEMICAL INDUSTRY LLC Free format text: FORMER OWNER: XINJIANG ZHONGTAI CHEMICAL CO., LTD. Effective date: 20150427 |
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Effective date of registration: 20150427 Address after: Yimin 830009 West Street in the Xinjiang Uygur Autonomous Region Urumqi City No. 1868 Patentee after: Xinjiang Huatai Heavy Chemical Co., Ltd. Address before: 830009 No. 39 Yangcheng Lake Road, Urumqi economic and Technological Development Zone, the Xinjiang Uygur Autonomous Region Patentee before: Xinjiang Zhongtai Chemical Co., Ltd. |
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Granted publication date: 20141126 Termination date: 20210528 |