CN104497186A - Premixing method and device of catalysts for preparing butadiene rubber - Google Patents
Premixing method and device of catalysts for preparing butadiene rubber Download PDFInfo
- Publication number
- CN104497186A CN104497186A CN201410721611.5A CN201410721611A CN104497186A CN 104497186 A CN104497186 A CN 104497186A CN 201410721611 A CN201410721611 A CN 201410721611A CN 104497186 A CN104497186 A CN 104497186A
- Authority
- CN
- China
- Prior art keywords
- promotor
- agitating vane
- pipeline
- polybutadiene rubber
- premixed device
- 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.)
- Granted
Links
Landscapes
- Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
The invention discloses a premixing method and device of catalysts for preparing butadiene rubber. The method and device are characterized in that a power mechanism consisting of a motor and a speed reducer is mounted at the outer part of a pre-mixer; agitating blades are mounted on a rotating shaft at the output end of the speed reducer; the rotating shaft and the agitating blades are mounted in a bend at one end close to an inlet of a polymerizing kettle; a main catalyst and a cocatalyst are aged through a static mixer and then enter a pipeline between a butadiene solution inlet and an agitating blades area, and another cocatalyst or a plurality of cocatalysts are aged through the ageing kettle and then enter the agitating blades area. According to the method and device, the pre-mixer is additionally arranged in front of the polymerizing kettle, and the rotating shaft and the agitating blades arranged in the pre-mixer can be used for quickly mixing and shearing materials; therefore, a plurality of catalysts can be quickly mixed in the pipeline pre-mixer; a multi-layer agitating mechanism, a near-wall agitating mechanism and an equal-diameter pipeline are arranged in the agitating system to decrease dead areas of flowing, so that the retention time distribution is narrowed, the average retention time is controlled through the rotating speed, and as a result, the adhering and blocking in the pre-mixer can be decreased, and the polymerizing process can be performed for a long cycle.
Description
Technical field
The present invention relates to and prepare cis-1,4-polybutadiene rubber, be specifically related to a kind of catalyst premixing method and apparatus preparing cis-1,4-polybutadiene rubber.
Background technology
The production technology of domestic cis-1,4-polybutadiene rubber, through practice for many years, has achieved the achievement attracted people's attention in catalyzer, technique and engineering.But compare with state-of-the-art technology, still there is energy consumption (mainly steam) and unit consumption (mainly solvent) is higher, the problems such as some inner quality not high (as low molecular weight fraction too much causes that molecular weight distribution is wide and mooney viscosity reduces, branched structure is too high, microgel content is high).
Chemically the viewpoint of engineering is analyzed, and the major reason producing these problems is that in polymeric kettle, heat transfer and mixing two large problems not yet seek more reasonably solution.Key to the issue is because cis-1,4-polybutadiene rubber polymer industry stirring tank generally adopts the limitation of inside and outside single ribbon and inclined frame two kinds of agitator design, not ideal enough to the short mix effect of catalyzer bottom first still, and there is stagnant wake.
Produce for nickel polymerized BR, Primary Catalysts adopts nickel naphthenate (being called for short Ni), and a kind of promotor is triisobutyl aluminium (being called for short Al), and another kind of promotor is boron trifluoride ethyl ether complex (being called for short B).Adopt different preparation process, polymerization activity is different.Conventional aging has ternary ageing, and (Ni, B, Al are mixed with solution respectively, add by a graded again), two binary ageing (Al is mixed ageing with Ni, B component according to a certain percentage respectively), add (by Ni, Al mixing ageing with rare B is mono-, B directly adds polymeric kettle after being mixed with solution), wherein rare B is mono-adds aging application at most.
Bottom first still, rare B will with in the butadiene solution containing Al-Ni and still the glue of the suitable viscosity of tool contact, carry out the fluid chemical field that three bursts of temperature, viscosity and density have very big-difference, its mixing time can than etc. viscosity homopycnal flow body extension 2 times, thus in rare B and butadiene solution (containing Al-Ni) intersection, short period of time far can not reach abundant mixing, cause Al/B (or Al/Ni) off-target proportioning greatly, add the temperature in the kettle caused due to mixture strength difference uneven, have impact on polymerization effect.Because the mixing of catalyzer is bad, may cause the too high of gel content in subsequent reactions still, kiss-coating is serious, causes normal production cycles to shorten.
Before polymeric kettle, adopt premix still object to be: the mixing of (1) strengthening material, particularly solve the local over-concentration of the first still catalyzer of polymeric kettle and the irregular problem of dispersion; (2) stable catalytic active center can be formed; (3) polymeric kettle reacting balance can be made, be conducive to the control of polymerization process, suppress the generation of gel, constant product quality.
Premix still to very important along fourth many stills continuous polymerization process because before entering polymeric kettle monomer, solvent, catalyzer mixes with the ratio of additive etc. is vital.But for preventing material from producing polyreaction in premix still, all will strictly limit the volume of premix still and residence time of material, otherwise premix still will become prepolymerization kettle, this acts on the measure far apart failed to agree, and must cause the out of control of product molecule parameter.
Publication number is that CN1814634 and CN101885794 Chinese patent literature discloses preparation 1, the premixing process of 4-polybutadiene rubber, this technique adds a premix still before first polymeric kettle, its type is stirring autoclave, be provided with anchor formula stirring rake, the residence time of catalyzer in premix still is at about 12 ~ 20min.
Daqing Petroleum Institute's Master's thesis (2006, Wang Wenying) disclose the premixing process of polymerizing butadiene, nickel naphthenate first mixes in a static mixer with the boron trifluoride ethyl ether complex after dilution, pipeline again through certain length mixes at another static mixer with butadiene solution, form the ternary ageing liquid of Ni-B-Bd, then enter and stir premix still.Triisobutyl aluminium is entered separately by another pipeline and stirs premix still, and its residence time controls within the scope of 12 ~ 18min.
The pre-mixing apparatus adopted in above-mentioned disclosed patent documentation, Problems existing, one is that premix still volume is large, and catalyzer residence time in premix still is long, and divinyl is polymerized, and that causes high adhesive aggregation compound sticks the whole premix still of blocking; Two is adopt anchor formula stirring rake, and its mixing efficiency is very low; Three is there is flow dead in premix still, and cause residence time destribution very wide, some divinyl that the residence time is longer in premix still are polymerized under catalyst action, and high sticky material is easily attached on still wall and discharge port.Adopt above-mentioned method or device, premix still easily blocks, and is difficult to reach desirable effect.
Summary of the invention
In order to solve Problems existing in background technology, the object of the present invention is to provide a kind of catalyst premixing method and apparatus preparing cis-1,4-polybutadiene rubber, realizing the long-term operation of the efficient premix poly-unit of catalyzer.
The technical solution used in the present invention is:
One, a kind of catalyst premixing method preparing cis-1,4-polybutadiene rubber
By the mixture of Primary Catalysts, a kind of promotor and butadiene solution, while being transported to from the bend pipe of pipeline premixed device one end the agitating vane be arranged in pipeline premixed device together, with be positioned at the another kind of promotor of agitating vane area entry or two kinds of promotors after quick premix, enter into polymeric kettle bottom inlet from the outlet of pipeline premixed device.
The mixture of described Primary Catalysts, a kind of promotor and butadiene solution, and another kind of promotor or two kinds of promotors quick premix in pipeline premixed device, the residence time is 1 ~ 60 second.
The rotating speed of described agitating vane is 100-1500rpm.
Two, a kind of catalyst premixing device preparing cis-1,4-polybutadiene rubber
Pre-mixing apparatus is pipeline premixed device, and it comprises bend pipe and actuating unit, it is outside that the actuating unit be made up of motor and speed reducer is arranged on pipeline premixed device, the output terminal connection rotating shaft of step-down gear, agitating vane is equipped with in rotating shaft, rotating shaft and agitating vane are arranged in the bend pipe of polymeric kettle entrance one end, Primary Catalysts and a kind of promotor after static mixer ageing entry to mixed solution on the pipeline between the pipeline premixed device entrance and agitating vane region of butadiene solution, the promotor entrance of another kind of promotor is positioned at agitating vane region, or a kind of promotor and another kind of promotor enter in agitating vane region through promotor entrance after aging reactor ageing.
The internal diameter of described bend pipe is same diameter.
Described agitating vane polymeric kettle Way in is pointed to fluid pushing direction.
Described agitating vane is single or multiple lift blade.
Described agitating vane is the combination of radial flow blade, axial flow blade or radial flow blade and axial flow blade.
The beneficial effect that the present invention has is:
Cis-1,4-polybutadiene rubber catalyst premixing method and apparatus of the present invention, multiply catalyzer short mix in pipeline premixed device can be made, stirring system is provided with in pipeline premixed device, by multilayer stirring, nearly wall stirring mechanism and equal diameter pipeline, the present invention makes flow dead reduce, residence time destribution narrows, mean residence time can be controlled by rotating speed, obviously alleviate the felt jam situation in premixed device, make polymerization process can long-term operation, the present invention can produce effective rapid stirring mixing effect to catalyzer, promotes the quality product of cis-1,4-polybutadiene rubber.
Accompanying drawing explanation
Fig. 1 is a kind of catalyst premixing setting drawing (adopt rare B is mono-adds preparation process) preparing cis-1,4-polybutadiene rubber of the present invention.
Fig. 2 is a kind of catalyst premixing setting drawing (adopting two binary catalyst aging) preparing cis-1,4-polybutadiene rubber of the present invention.
Fig. 3 is the catalyst premixing setting drawing (adopt rare B is mono-adds preparation process) that another kind of the present invention prepares cis-1,4-polybutadiene rubber.
In figure: 1, pipeline premixed device entrance, 2, motor, 3, step-down gear, 4, promotor entrance, 5, agitating vane, 6, the outlet of pipeline premixed device, 7, rotating shaft, 8, polymeric kettle, 9, a kind of promotor, 10, butadiene solution, 11, Primary Catalysts, 12, another kind of promotor, 13, static mixer, 14, Primary Catalysts entrance, 15, aging reactor.
Embodiment
Below in conjunction with drawings and Examples, the invention will be further described.
As shown in Figure 1 and Figure 2, pre-mixing apparatus of the present invention is pipeline premixed device, and it comprises bend pipe and actuating unit; It is outside that the actuating unit be made up of motor 2 and step-down gear 3 is arranged on pipeline premixed device, and the output terminal connection rotating shaft 7 of step-down gear 3, rotating shaft 7 is equipped with agitating vane 5, and rotating shaft 7 and agitating vane 5 are arranged in the bend pipe of polymeric kettle 8 entrance one end.As adopted, rare B is mono-adds preparation process, Primary Catalysts 11(Ni) and a kind of promotor 9(Al) after static mixer 13 ageing entry to mixed solution on the pipeline between the pipeline premixed device entrance 1 and agitating vane 5 region of butadiene solution 10, another kind of promotor 12(B) promotor entrance 4 be positioned at agitating vane 5 region (Fig. 1).
As adopted two binary catalyst aging, Al is mixed ageing with Ni, B component according to a certain percentage respectively.Primary Catalysts 11(Ni) and a kind of promotor 9(Al) after static mixer 13 ageing entry to mixed solution on the pipeline between the pipeline premixed device entrance 1 and agitating vane 5 region of butadiene solution 10, a kind of promotor 9(Al) with another kind of promotor 12(B) enter in agitating vane 5 region (Fig. 2) through promotor entrance 4 after aging reactor 15.
The internal diameter of described bend pipe is same diameter, reduces pipeline diameter and the flow dead of causing such as to reduce, and its volume is connected 0.05% ~ 1.5% of polymeric kettle volume about for it.。
Described agitating vane 5 is single or multiple lift blade, and as preferably, described agitating vane preferably adopts 2 ~ 6 layers of blade.
Agitating vane 5 can adopt multiple different configuration, rational configuration and distribution mode, shear-mixed efficiency can be made to improve, the effect that residence time destribution narrows.Agitating vane can be radial flow blade, or axial flow blade, or the combination of radial flow blade and axial flow blade.Agitating vane to fluid pushing direction downstream-directed.
As preferably, described agitating vane can adopt the combination of radial flow blade and axial flow blade.Radial flow blade can strengthen shearing and mixing of materials, axial flow blade can strengthen the impellent of axial flow, material is moved in the mode close to plug flow, residence time destribution is narrowed, be easy to control the residence time of material in premixed device, reduce or avoid the generation of high viscosity polyhutadiene and stick.
The direct result using premixed device is that catalyst premixing efficiency is high, and gel obviously improves, and quality product rises, and indirect consequence is that pipeline does not block and can use for a long time, extends polymerization life cycle.
Method for pre mixing of the present invention:
As shown in Figure 1 and Figure 2, by the mixture of Primary Catalysts 11, a kind of promotor 9 and butadiene solution 10, while being transported to from the bend pipe of pipeline premixed device entrance 1 one end the agitating vane be arranged in pipeline premixed device together, after crossing premix with the another kind of promotor 12 or a kind of promotor 9 that are positioned at agitating vane area entry with the mixed flow stock-traders' know-how of another kind of promotor 12 after aging reactor 15, enter into polymeric kettle bottom inlet from pipeline premixed device outlet 6.
The mixture of described Primary Catalysts, a kind of promotor and butadiene solution, and the mixed solution after another kind of promotor or a kind of promotor 9 and the ageing of another kind of promotor 12, in pipeline premixed device, the residence time is 1 ~ 60 second.
The rotating speed of described agitating vane is 100-1500rpm.
Be provided with rotating shaft and agitating vane in pipeline premixed device, by motor and speed reducer or frequency transformer, adjusting rotary speed, the rotating speed of agitating vane is 100-1500rpm.Adopt pipeline high-speed stirring, to cause shearing force higher in pipe, material is strongly stirred and mixes.By the change of mixing speed, the mean residence time of material in pipeline premixed device can be controlled.
Agitating vane diameter should close to pipe diameter, and both are than can between 0.6-0.99.As preferably, described diameter proportion is 0.8 ~ 0.95.The rotation of large diameter agitating vane, can strengthen the flowing that goes out close to tube wall and mixing, alleviate sticking of near-wall.Blade and tube wall gap less, better to the dispersion effect of material, simultaneously reduce material particles to the adhesion of tube wall; But gap is too small, require excessive to the manufacturing accuracy of the equipment such as axle and sealing.
Embodiment 1
As shown in Figure 1, nickel catalyst premixing process of the present invention, adopts that rare B is mono-adds preparation process.Primary Catalysts (Ni) and the first promotor (Al), by Primary Catalysts entrance 14, enter through at butadiene solution main line, after entering pipeline premixed device by pipeline premixed device entrance 1 again, second promotor (B) enters pipeline premixed device by promotor entrance 4, carry out short mix in pipeline premixed device after, export 6 by pipeline premixed device and flow out, enter polymeric kettle from polymeric kettle lower entrances.
It is outside that the actuating unit be made up of motor 2 and step-down gear 3 is arranged on pipeline premixed device, the output terminal connection rotating shaft 7 of step-down gear 3, and drive shaft 7 rotates, and pipeline premixed device is stretched in rotating shaft 7 from the center bottom pipeline premixed device inner.
In the present embodiment, stirring rake is three layers of stirring rake, arranges from rotating shaft 7 end, adopts radial flow oar, radial flow oar and Axial flow impeller respectively.Agitating vane 5 is 10mm with the gap of pipeline premixed device inwall.
Embodiment 2
As shown in Figure 3, the present embodiment and the difference of embodiment 1 are only the different of butadiene solution Way in and stirring rake form, in this example, butadiene solution enters from shaft end, in the present embodiment, agitating vane is still three layers of stirring rake, arrange from shaft end, adopt Axial flow impeller, radial flow oar and radial flow oar respectively.
Application examples 1:
In cis-1,4-polybutadiene rubber industrial polymerisation flow process, the method for pre mixing proposed according to the present invention and device embodiment, carry out technical grade test simulation to process.Its processing condition are: polymeric kettle temperature of lower 70 DEG C, feeding temperature 36 ~ 42 DEG C, butadiene solution concentration 13.6g/100ml, catalyst formulation: Ni/ divinyl ratio is 1.0, Al/ divinyl ratio is 0.21, B/ divinyl ratio is 0.6.The pre-mixing apparatus of the configuration embodiment of the present invention 1, the rotating speed of stirring rake is 600rpm.
After pipeline premixed device comes into operation, there is larger change in processing condition, the oil-filled amount in polymeric kettle significantly reduces, and reaction is stablized with mooney viscosity.Pipeline premixed device reaches 869 hours working time.
Under B agent consumption reduces the corresponding situation in a slight decrease of 33.3%, Al agent consumption, it is 0.44 that Al/B rises to than by original 0.36, and mooney viscosity is normal, and response intensity was higher than the past.
Application examples 2:
The pre-mixing apparatus of the configuration embodiment of the present invention 1, the rotating speed of stirring rake is 700rpm.
B dilution agent oil consumption is reduced to 0.45 from 0.6, and paradigmatic system is still stablized, and illustrates that catalyzer obtains reasonable dispersion in premixed device, does not need dilution; Also make side effect-dirty oil be unlikely to occur simultaneously.Reclaim divinyl than few when not using premix to equip, return the contrast of fourth amount by the forward and backward average per tour that comes into operation, before coming into operation, fourth amount is returned in average per tour is 15.11 tons, and after coming into operation, fourth amount is returned in average per tour is 13.82 tons, and average per tour reduces back fourth amount 1.29 tons.Explanation transformation efficiency significantly improves, and output rises.
Claims (8)
1. prepare the catalyst premixing method of cis-1,4-polybutadiene rubber for one kind, it is characterized in that: by the mixture of Primary Catalysts, a kind of promotor and butadiene solution, while being transported to from the bend pipe of pipeline premixed device one end the agitating vane be arranged in pipeline premixed device together, with be positioned at the another kind of promotor of agitating vane area entry or two kinds of promotors after quick premix, enter into polymeric kettle bottom inlet from the outlet of pipeline premixed device.
2. a kind of catalyst premixing method preparing cis-1,4-polybutadiene rubber according to claim 1, it is characterized in that: the mixture of described Primary Catalysts, a kind of promotor and butadiene solution, the quick premix in pipeline premixed device with another kind of promotor or two kinds of promotors, the residence time is 1 ~ 60 second.
3. a kind of catalyst premixing method preparing cis-1,4-polybutadiene rubber according to claim 1, is characterized in that: the rotating speed of described agitating vane is 100-1500rpm.
4., for a kind of catalyst premixing device preparing cis-1,4-polybutadiene rubber of method described in claim 1, it is characterized in that: pre-mixing apparatus is pipeline premixed device, and it comprises bend pipe and actuating unit, it is outside that the actuating unit be made up of motor (2) and step-down gear (3) is arranged on pipeline premixed device, the output terminal connection rotating shaft (7) of step-down gear (3), agitating vane (5) rotating shaft (7) is equipped with, rotating shaft (7) and agitating vane (5) are arranged in the bend pipe of polymeric kettle (8) entrance one end, Primary Catalysts (11) and a kind of promotor (9) entry to mixed solution after static mixer (13) ageing is positioned on the pipeline between the pipeline premixed device entrance (1) of butadiene solution (10) and agitating vane (5) region, the promotor entrance (4) of another kind of promotor (12) is positioned at agitating vane (5) region, or a kind of promotor (9) and another kind of promotor (12) enter in agitating vane (5) region through promotor entrance (4) after aging reactor (15) ageing.
5. a kind of catalyst premixing device preparing cis-1,4-polybutadiene rubber according to claim 4, is characterized in that: the internal diameter of described bend pipe is same diameter.
6. a kind of catalyst premixing device preparing cis-1,4-polybutadiene rubber according to claim 4, is characterized in that: described agitating vane (5) to fluid pushing direction point to polymeric kettle (8) Way in.
7. a kind of catalyst premixing device preparing cis-1,4-polybutadiene rubber according to claim 4, is characterized in that: described agitating vane (5) is single or multiple lift blade.
8. a kind of catalyst premixing device preparing cis-1,4-polybutadiene rubber according to claim 4, is characterized in that: described agitating vane (5) is radial flow blade, the combination of axial flow blade or radial flow blade and axial flow blade.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410721611.5A CN104497186B (en) | 2014-12-03 | 2014-12-03 | Premixing method and device of catalysts for preparing butadiene rubber |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410721611.5A CN104497186B (en) | 2014-12-03 | 2014-12-03 | Premixing method and device of catalysts for preparing butadiene rubber |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104497186A true CN104497186A (en) | 2015-04-08 |
| CN104497186B CN104497186B (en) | 2017-05-17 |
Family
ID=52938651
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410721611.5A Active CN104497186B (en) | 2014-12-03 | 2014-12-03 | Premixing method and device of catalysts for preparing butadiene rubber |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104497186B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107540766A (en) * | 2016-06-23 | 2018-01-05 | 中国石油化工股份有限公司 | A kind of method of catalyst pre-contact device and catalyst pre-contact for alkene continuous polymerization |
| CN107537408A (en) * | 2016-06-23 | 2018-01-05 | 中国石油化工股份有限公司 | A kind of method of catalyst pre-contact device and catalyst pre-contact for alkene continuous polymerization |
| CN114307840A (en) * | 2022-01-08 | 2022-04-12 | 安徽省农业科学院棉花研究所 | Organic formula fertilizer hot returning charge equipment |
| CN116726758A (en) * | 2023-08-14 | 2023-09-12 | 振华新材料(东营)有限公司 | Catalyst premixing method and device for preparing butadiene rubber |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1334274A (en) * | 2000-07-26 | 2002-02-06 | 陶氏康宁有限公司 | Polymerization reactor and method |
| CN101885794A (en) * | 2009-05-14 | 2010-11-17 | 关震宇 | Method for synthesizing polybutadiene rubber by adopting catalyst premixing process |
| CN202054768U (en) * | 2011-03-21 | 2011-11-30 | 中国石油化工股份有限公司 | Premixing kettle, premixing device and multi-kettle polymerizing equipment for producing isoprene rubber |
-
2014
- 2014-12-03 CN CN201410721611.5A patent/CN104497186B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1334274A (en) * | 2000-07-26 | 2002-02-06 | 陶氏康宁有限公司 | Polymerization reactor and method |
| CN101885794A (en) * | 2009-05-14 | 2010-11-17 | 关震宇 | Method for synthesizing polybutadiene rubber by adopting catalyst premixing process |
| CN202054768U (en) * | 2011-03-21 | 2011-11-30 | 中国石油化工股份有限公司 | Premixing kettle, premixing device and multi-kettle polymerizing equipment for producing isoprene rubber |
Non-Patent Citations (1)
| Title |
|---|
| 王文清等: "聚丙烯催化剂预混罐的剖析", 《齐鲁石油化工》 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107540766A (en) * | 2016-06-23 | 2018-01-05 | 中国石油化工股份有限公司 | A kind of method of catalyst pre-contact device and catalyst pre-contact for alkene continuous polymerization |
| CN107537408A (en) * | 2016-06-23 | 2018-01-05 | 中国石油化工股份有限公司 | A kind of method of catalyst pre-contact device and catalyst pre-contact for alkene continuous polymerization |
| CN114307840A (en) * | 2022-01-08 | 2022-04-12 | 安徽省农业科学院棉花研究所 | Organic formula fertilizer hot returning charge equipment |
| CN114307840B (en) * | 2022-01-08 | 2022-09-16 | 安徽省农业科学院棉花研究所 | Organic formula fertilizer hot returning charge equipment |
| CN116726758A (en) * | 2023-08-14 | 2023-09-12 | 振华新材料(东营)有限公司 | Catalyst premixing method and device for preparing butadiene rubber |
| CN116726758B (en) * | 2023-08-14 | 2023-10-20 | 振华新材料(东营)有限公司 | Catalyst premixing method and device for preparing butadiene rubber |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104497186B (en) | 2017-05-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104497186A (en) | Premixing method and device of catalysts for preparing butadiene rubber | |
| CN205042452U (en) | Percussion flow heterogeneous reaction ware | |
| CN202054768U (en) | Premixing kettle, premixing device and multi-kettle polymerizing equipment for producing isoprene rubber | |
| CN202343133U (en) | Coating homogenization system | |
| CN203556354U (en) | Novel polymeric kettle | |
| CN204073997U (en) | A kind of propeller-blade | |
| CN201799274U (en) | Reaction kettle | |
| CN204074075U (en) | A kind of chemical reaction kettle | |
| CN217120252U (en) | Butadiene rubber polymerization cauldron | |
| CN101880345A (en) | Pre-mixing process in rare-earth isoprene rubber production process | |
| CN214287964U (en) | Reaction system for preparing water-based strippable coating | |
| CN216367463U (en) | Liquid feed stirring device | |
| CN202778471U (en) | Drug intermediate reaction kettle with excellent stirring performance | |
| CN204699690U (en) | Reactor fan leaf type agitator | |
| CN104292370B (en) | A kind of propylene continuous alternating temperature prepolymerization device and prepolymerization technology of propylene | |
| CN201239612Y (en) | Static state fluid mixer | |
| CN204017734U (en) | A kind of composite stirring equipment | |
| CN208776630U (en) | A kind of continuous alternating temperature prepolymerization device of propylene | |
| CN104525016B (en) | A kind of agitating device for gas-liquid mixed reactor | |
| CN201415984Y (en) | Premixing device for rare-earth isoprene rubber production | |
| CN112387177B (en) | Filling system suitable for solid resistance reducing agent and solid thickening agent | |
| CN102924260A (en) | Technique and device for continuously producing stearate by low-temperature dry process | |
| CN204583180U (en) | For the synthesis of the reactor of insulation material | |
| CN207413236U (en) | A kind of all-round flow guiding type blender | |
| CN202478897U (en) | Mixing device applied to high-viscosity liquid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |