CN101054447A - Steam stripping coacervation and separation device for polymer solution and separation method thereof - Google Patents
Steam stripping coacervation and separation device for polymer solution and separation method thereof Download PDFInfo
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Abstract
A stripping condensing separator of a polymer solution and the separating method thereof are provided. The inventive apparatus switches the traditional condensation with two vessels to horizontal flokcculator which is separated by clapboard into A and B sections, which mainly comprises: two eccentric agitators, three liquid spray jets, venturi mixer, concentrator and etc. The polymer solution has a mass concentration of 5-80%, a flokcculator A section temperature of 70-100 DEG C, a gage pressure of 0.01-0.05 MPa, B section temperature of 90-110 DEG C, a a gage pressure of 0.01-0.05 MPa. The volume flux of the hot water volume flux in the flokcculator to polymer solution volume flux is 2-15. It can effectively save the cost, largely reduce the energy consumption, simplifies the operation and control, gets a good condensation separation effect, which is especially suitable for the solution separation of synthetic rubber, resin and plastic polymer.
Description
Technical field
The invention belongs to the polymer production technical field, more particularly relate to the steam stripping coacervation and separation device of polymers solns such as synthetic rubber, synthetic resins and plastics and the improvement of separation method thereof.
Background technology
The polymers soln that solution polymerization process obtains generally adopts in hot water the steam stripping coacervation method with polymkeric substance and separated from solvent at present.Extensively adopt many stills condensation technique (two or more stirring tank series connection) at present, on flocculating result and energy consumption, be better than early stage single still cohesion and tower condensation technique [Yu Leshun, China Synthetic Rubber Industry, 1978,1 (5), 1; Beijing Yanshan Petrochemical Company triumph chemical plant, China Synthetic Rubber Industry, 1978,1 (4), 1; Zhao Duoshan, China Synthetic Rubber Industry, 1986,9 (5), 318; Xu Shiai etc., China Synthetic Rubber Industry, 1997,20 (6), 369].Wherein, each placed in-line cohesion still all is vertical stirring tank, and the ratio H/D of its height H and diameter D so just has to adopt the multilayer agitator about 3.On producing, the agitator motor power of 60～100 cubic metres of cohesion stills is 75kW, and the energy consumption of average unit volume is about 1kW/m
3About, be quite high [Yu Leshun, China Synthetic Rubber Industry, 1980,3 (3), 145].In addition, must adopt large diameter pipeline to come delivering hot water and micelle between the placed in-line cohesion still by the liquid level difference between still and the still, pressure difference or high-power particle pump, this not only makes equipment install and operation control complexity and energy consumption increase, and occurs easily influencing normal running because of the obstruction of micelle.
The Production Flow Chart that has for increase micelle residence time of the 2nd still (with the 3rd still) to increase flocculating result [GB1172797 (1969)], on the pipeline between two cohesion stills, set up the dense device of carrying of particular design, from micelle water, tell a certain amount of hot water.Yet this carries not only complex structure but also easily by the normal running of micelle congestion affects of dense device.
The Production Flow Chart that also has is in order further to save steam, and the rising gas (the water vapor quality accounts for about 80%) of the 2nd cohesion still is directly introduced the 1st cohesion still as the part of heating steam and energy-conservation [US3076795 (1963)].So just have to the 2nd cohesion still pressure is improved, with the pressure that the liquid level that overcomes the 1st cohesion still produces, this makes two connections between still difficulty more.
Therefore, need be improved existing pair of still or many stills condensation technique from saving facility investment and the energy consumption and the control angle that simplifies the operation at present.
Summary of the invention
Purpose of the present invention is to overcome above-mentioned shortcoming and defect, and the steam stripping coacervation and separation device and the separation method thereof of a kind of polymkeric substance and solvent is provided.It can effectively save facility investment, the save energy that cuts down the consumption of energy greatly, simplifies the operation and CONTROL PROCESS, obtains good agglomeration separation effect.
In order to achieve the above object, the present invention changes traditional two or more placed in-line vertical stirring cohesion still into one horizontal stirring cohesion still, the centre is divided into two condensation regions (still) with dividing plate, further saves facility investment and energy consumption and the control that simplifies the operation when reaching two stills or many stills flocculating result.
The present invention includes have import and polymer beads water out and about be divided into the horizontal knockouts in A district and B district, be installed in the agitator in A district and B district respectively, be installed in three fluid tips of horizontal knockouts import, be connected the polymers soln pipeline on three fluid tips, be connected the B district rising gas pipeline above the horizontal knockouts B district, the venturi mixer that is connected with B district heating steam pipeline with B district rising gas pipeline, be connected the B district heating steam pipeline of bottom, horizontal knockouts B district, be connected the A district rising gas pipeline above the horizontal knockouts A district, be connected the condenser on the A district rising gas pipeline, be undertaken on the separation sieve below the polymer beads water out, be connected the hot-water cylinder below the separation sieve, be installed in the dense device of carrying below the horizontal knockouts A district, with carry the dense water pipeline of carrying that dense device is connected, be connected the hot water pump of carrying on the dense water pipeline, be connected to circulating hot water pipeline and hot water line between hot water pump and polymers soln pipeline and the horizontal knockouts A district.Hot water line, circulating hot water pipeline and carry and hot water flow meter, circulating hot water under meter are installed respectively on the dense water pipeline and carry concentrated stream amount meter, hot-water cylinder and carrying between the dense water pipeline connects with pipeline.Venturi mixer also is connected with the steam jacket of pipeline with three fluid tips.
An agitator is installed respectively in the A district of horizontal knockouts and the B district, center fixed dividing plate, perforate is arranged at the bottom of dividing plate, the side of dividing plate is installed with flashboard, connecting one on the flashboard has the gland sealed screw rod that flashboard can be moved up and down at wall, regulates the size of perforate according to the size of throughput.Two agitators are all installed near dividing plate.Two agitators are axial flow type.
Produce certain negative pressure when venturi mixer is flowed through in heating steam, the rising steam in knockouts B district is sucked and the chuck that mixes afterwards by three fluid tips sprays into the heating steam of knockouts A district as steam stripping coacervation.Like this, the rising steam in available pyritous B district heats the A district, and prevents to cause thus the pressure in B district to raise, thereby saves energy.
Three fluid tips are made up of static mixer and steam jacket, and polymers soln and circulating hot water mix in static mixer, by in the chuck from the water vapor preheating of venturi mixer, the three sprays into the A district of knockouts together then.The polymers soln preheating not only helps reducing fluid viscosity and promotes to mix, and further produces cutting and dissemination in the exit of nozzle generation shearing force, promotes flocculating result.Static mixer has 5～20 mixed cells.
Traditional stirring cohesion still majority all adopts single fluid (polymers soln) nozzle, needs the shearing force cutting and the dispersing polymer solution that rely on stronger mechanical stirring to produce, therefore mechanical stirring is required very highly, so that mixing speed and power are all very high.It is three fluid tips of core with the static mixer that the present invention has adopted, itself need not just can effectively cut and disperse to polymers soln by mechanical stirring, change into vertical stirring tank horizontal in addition, liquid level is reduced to below 1 by about 3 with the ratio in still footpath, only needs the individual layer agitator to keep the normal suspension of polymer beads and flow under lower rotating speed and power and gets final product.Therefore, power of agitator consumption of the present invention is only stirred about 1/3 of cohesion still for traditional vertical.
The agitator that the present invention adopts is axial flow type such as open-type hinged joint turbine agitator, oar type propeller agitator etc.Agitator speed is 30～100r/min, is eccentric the installation, because its asymmetry need not baffle plate and just can obtain good mixing effect.
Carry dense device by the bigger cylindrical metal silk screen of diameter with support the wire cylinder mould that its metal cage is formed, the mesh of wire cloth is less than 4 * 4mm.Blowback steam or the nitrogen mouth that prevents that micelle from stopping up is equipped with in the bottom of wire cylinder mould, and blowback can be regularly or not timing, also can be pulsed.Carrying dense device can filter out polymer beads, makes the hot water in A district pass through wire cloth
Enter hot water line and enter hot water pump again, the hot water amount who enters the B district is reduced, so also just increased the residence time of polymer beads, so that further improved flocculating result in the B district of higher temperatures.
The present invention also provides the steam stripping flocculation separation method of a kind of polymkeric substance and solvent:
To be 5～80% polymers soln the static mixer of nozzle mix after spray into knockouts A district in three fluid tip ingress with hot water from hot water pump by pipeline to mass concentration, and the hot water volumetric flow rate that enters horizontal knockouts is controlled to be 2～15 with the ratio of polymers soln volumetric flow rate.
The heating steam venturi mixer of flowing through produces certain negative pressure, the rising steam in knockouts B district sucked and mixes the chuck of back by three fluid tips and spray into of the heating steam of knockouts A district as steam stripping coacervation, the while at the nozzle chuck with the polymers soln preheating.The temperature of controlling horizontal knockouts A district is that 70～100 ℃, gauge pressure are 0.01～0.05MPa, and control B district temperature is that 90～110 ℃, gauge pressure are 0.01～0.05MPa.B district temperature is controlled by the heating steam of B district.
In the relatively low A district of temperature, advanced condenser condenses layering with corresponding water vapor by the vapour phase pipeline by the isolating solvent of stripping and reclaim.The polymer beads that is condensed in the A district enters the high relatively B district of temperature in company with the bottom perforate of hot water by central dividing plate and further enters separation sieve with hot water from outlet and told in the cohesion back.Solvent quality content in the polymer beads is less than 1% (butt) at this moment.
In order further to improve flocculating result, the part hot water in A district directly can be entered hot water pump by carrying dense device, the hot water amount who enters the B district is reduced, so also just increased the residence time of polymer beads, so that improved flocculating result in the B district of higher temperatures.This part hot water can be by the under meter dominant discharge, and the hot water that comes out from a hot water pump part as required enters nozzle, and the control of another part under meter directly enters knockouts A district.
Theoretical foundation of the present invention is as follows:
Mechanism [Yu Leshun according to agglomeration process, China Synthetic Rubber Industry, 1979,2 (4), 289], the 1st stage at agglomeration process is that the constant speed agglomeration phase claims the agglomeration phase of vaporizing again, and about solvent more than 95% is steamed by stripping by more a spot of water vapor (mass ratio of solvent and water is less than 0.5 in the vapour phase) in the A district of lesser temps in the polymers soln (mass concentration 10～20% of polymkeric substance), and this stage is controlled by heat transfer rate.The B district that the polymer beads that contains a small amount of solvent (mass concentration 10～40%) enters comparatively high temps carries out the 2nd stage of agglomeration process, the agglomeration phase that promptly slows down just spreads agglomeration phase, in this stage, the solvent of polymer beads inside need rely on molecular diffusion to be delivered to particle surface and be steamed by stripping, and cohesion speed is controlled by velocity of diffusion.Therefore, the B district needs higher temperature to promote the 2nd stage of the agglomeration process agglomeration phase that promptly slows down just to spread the carrying out of agglomeration phase.Knockouts of the present invention is according to the mechanism design of agglomeration process.
According to liquid agitation theory (J.Y. Ou Shu, fluid hybrid technology, Chemical Industry Press, 217,1991), for the liquid of equal volume, when the ratio of liquid height and diameter was reduced to 1 by 2, its mixing speed can reduce 1 times, and power of agitator can reduce 4 times.Therefore the present invention changes traditional vertical stirring tank into horizontal stirring tank and can save more energy.
Task of the present invention comes to this and finishes.
The present invention can effectively save facility investment, cuts down the consumption of energy greatly, save energy, simplifies the operation and CONTROL PROCESS, obtains good cohesion, separating effect.During the steam stripping coacervation that can be widely used in polymkeric substance that solution polymerization process obtains and solvent separates.
Description of drawings
Fig. 1 is equipment of the present invention and process principle figure.
The implication of each label is as follows among Fig. 1: the horizontal knockouts of 1-, the 2-dividing plate, 3, the 4-agitator, 5-three fluid tips, 6-carries dense device, the 7-venturi mixer, 8-polymer beads water out, 9-separation sieve, the 10-hot-water cylinder, 11-hot water pump, 12-are carried concentrated stream amount meter, 13-circulating hot water under meter, 14-polymers soln pipeline, 15-carries dense water pipeline, 16-circulating hot water pipeline, and 17-directly advances the knockouts hot water line, 18-and polymers soln blended hot water line, 19-heating steam pipeline, the rising gas pipeline in 20-B district, 21-A district rising gas pipeline, the 22-condenser, 23-directly advances knockouts hot water flow meter, and 24-regulates the removable flashboard of dividing plate perforate, 25-heating steam pipeline.
Embodiment
The steam stripping coacervation and separation device of embodiment 1, a kind of polymers soln, as shown in Figure 1.
Present embodiment comprise have import and polymer beads water out 8 and about be divided into the horizontal knockouts 1 in A district and B district, be installed in the agitator in A district and B district respectively, be installed in three fluid tips 5 of horizontal knockouts 1 import, be connected the polymers soln pipeline 14 on three fluid tips 5, be connected the B district rising gas pipeline 20 above the horizontal knockouts 1B district, the venturi mixer 7 that is connected with other heating steam pipeline 19 with B district rising gas pipeline 20, be connected the B district heating steam pipeline 25 of bottom, horizontal knockouts B district, be connected the A district rising gas pipeline 21 above the horizontal knockouts 1A district, be connected the condenser 22 on the A district rising gas pipeline 21, be undertaken on the separation sieve 9 below the polymer beads water out 8, be connected the hot-water cylinder 10 below the separation sieve 9, be installed in the dense device 6 of carrying below the horizontal knockouts 1A district, with carry the dense water pipeline 15 of carrying that dense device 6 is connected, be connected the hot water pump of carrying on the dense water pipeline 15 11, be connected to circulating hot water pipeline 16 and hot water line 17 between hot water pump 11 and polymers soln pipeline 14 and the horizontal knockouts 1A district.Hot water line 17 and circulating hot water pipeline 16 are installed with hot water flow meter 23 and circulating hot water under meter 13 respectively and carry concentrated stream amount meter 12 with carrying on the dense water pipeline 15.Hot-water cylinder 10 and carrying between the dense water pipeline 15 connects with pipeline.Venturi mixer 7 also is connected with the chuck of pipeline with three fluid tips 5.
An individual layer agitator 3 and 4 are installed respectively in the A district of horizontal knockouts 1 and the B district, center fixed dividing plate 2, the bottom perforate of dividing plate 2 communicates A district and B district, the side of dividing plate 2 is installed with removable flashboard 24, this flashboard 24 is regulated the size of perforate by being moved up and down by the gland sealed screw rod according to the size of throughput.Two individual layer agitators 3 and 4 are all installed near dividing plate 2, its stir shaft apart from the distance of central dividing plate 2 less than 1/2 of this district's cylindrical shell length of straight flange.Two agitators 3 and 4 are axial flow type.
Produce certain negative pressure when flowing through venturi mixer 7, the rising steam 20 in knockouts B district is sucked and the chuck that mixes afterwards by three fluid tips 5 sprays into the heating steam of knockouts A district as steam stripping coacervation from the heating steam of heating steam pipeline 19.
Three fluid tips 5 are made up of static mixer and steam jacket, the polymers soln of autohemagglutination compound solution pipeline 14 and in static mixer, mix from the circulating hot water of circulating hot water pipeline 16, by in the chuck from the water vapor preheating of venturi mixer 7, the three sprays into the A district of knockouts together then.Static mixer has 5～20 mixed cells.
Carry dense device 6 by the bigger cylindrical metal silk screen of diameter with support the wire cylinder mould that its metal cage is formed, the mesh of wire cloth is less than 4 * 4mm.Blowback steam or the nitrogen mouth that prevents that micelle from stopping up is equipped with in the bottom of wire cylinder mould, and blowback can be regularly or not timing, also can be pulsed.Carrying dense device 6 can filter out polymer beads, make the hot water in A district enter hot water line 15, enter hot water pump 11 again, the hot water amount who enters the B district is reduced by wire cloth, so also just increased the residence time of polymer beads, so that further improved flocculating result in the B district of higher temperatures.This part hot water can be by under meter 12,13 and 23 controls.The hot water that comes out from hot water pump 11 part as required enters nozzle 5 by pipeline 18, and another part directly enters knockouts A district by pipeline 17 by under meter 23 controls.
It is three fluid tips 5 of core that present embodiment adopts with the static mixer, itself need not just can effectively cut and disperse to polymers soln by mechanical stirring, change into vertical stirring tank horizontal in addition, liquid level is reduced to below 1 by about 3 with the ratio in still footpath, only needs the individual layer agitator to keep the normal suspension of polymer beads and flow under lower rotating speed and power and gets final product.Therefore, power of agitator consumption is only stirred about 1/3 of cohesion still for traditional vertical.Agitator 3 and 4 is an axial flow type, as open-type hinged joint turbine agitator, oar type propeller agitator etc.Agitator 3 and 4 rotating speeds are at 30～100r/min, and eccentric the installation just can obtain good mixing effect because its asymmetry need not baffle plate.
Embodiment 1 can effectively save facility investment, cut down the consumption of energy greatly, simplifies the operation and controls, and obtains good agglomeration separation effect.During the steam stripping coacervation that can be widely used in the polymers soln that solution polymerization process obtains separates.
The steam stripping flocculation separation method of embodiment 2, a kind of polymers soln.Mass concentration is that 10 liters/hour of 15% rare-earth isoprene rubber glues enter nozzle 5 from pipeline 14, and sprays into the A district after 5 liters/hour hot water from pipeline 18 mixes by static mixer (as the SK type), and 50 liters/hour of hot water enter the A district from pipeline 17.Water vapor enters the A district again from the steam jacket that enters nozzle 5 after pipeline 19 and 20 mixes by Venturi 7, and the temperature in A district is that 85 ℃, gauge pressure are 0.02MPa, and B district temperature is 100 ℃, and gauge pressure is 0.02MPa.
From carrying the hot water that dense device 6 extracts out is 25 liters/hour, and the hot water pump rate of discharge is 55 liters/hour, from the solvent quality content that exports 8 effusive micelles less than 1% (butt).
The steam stripping flocculation separation method of embodiment 3, a kind of polymers soln.Mass concentration is that 20 liters/hour of 5% rare-earth isoprene rubber glues enter nozzle 5 from pipeline 14, and sprays into the A district after 2 liters/hour hot water from pipeline 18 mixes by static mixer (as the SK type), and 38 liters/hour of hot water enter the A district from pipeline 17.Water vapor enters the A district from pipeline 19 and 20 again by the steam jacket that enters nozzle 5 after Venturi 7 mixing, and the temperature in A district is 96 ℃, and gauge pressure is 0.04MPa; B district temperature is 106 ℃, and gauge pressure is 0.04MPa.
From carrying the hot water that dense device 6 extracts out is 20 liters/hour, and the hot water pump rate of discharge is 40 liters/hour, from the solvent quality content that exports 8 effusive micelles less than 1% (butt).
The steam stripping flocculation separation method of embodiment 4, a kind of polymers soln.Mass concentration is that 10 liters/hour of 25% rare-earth isoprene rubber glues enter nozzle 5 from pipeline 14, and sprays into the A district after 8 liters/hour hot water from pipeline 18 mixes by static mixer (as the SK type), and 50 liters/hour of hot water enter the A district from pipeline 17.Water vapour enters the A district from pipeline 19 and 20 again by the steam jacket that enters nozzle 5 after Venturi 7 mixing, and the temperature in A district is 70 ℃, and gauge pressure is 0.01MPa; B district temperature is 90 ℃, and gauge pressure is 0.01MPa.
From carrying the hot water that dense device 6 extracts out is 25 liters/hour, and the hot water pump rate of discharge is 58 liters/hour, from the solvent quality content that exports 8 effusive micelles less than 1% (butt).
The steam stripping flocculation separation method of embodiment 5, a kind of polymers soln.Mass concentration is that 8 liters/hour of 50% rare-earth isoprene rubber glues enter nozzle 5 from pipeline 14, and sprays into the A district after 12 liters/hour hot water from pipeline 18 mixes by static mixer (as the SK type), and 80 liters/hour of hot water enter the A district from pipeline 17.Water vapour enters the A district from pipeline 19 and 20 again by the steam jacket that enters nozzle 5 after Venturi 7 mixing, and the temperature in A district is 90 ℃, and gauge pressure is 0.03MPa; B district temperature is 103 ℃, and gauge pressure is 0.03MPa.
From carrying the hot water that dense device 6 extracts out is 40 liters/hour, and the hot water pump rate of discharge is 92 liters/hour, from the solvent quality content that exports 8 effusive micelles less than 1% (butt).
The steam stripping flocculation separation method of embodiment 6, a kind of polymers soln.Mass concentration is that 5 liters/hour of 80% rare-earth isoprene rubber glues enter nozzle 5 from pipeline 14, with spray into the A district after 10 liters/hour hot water from pipeline 18 mixes by static mixer (as the SK type), 65 liters/hour of hot water enter the A district from pipeline 17, water vapour enters the A district from pipeline 19 and 20 again by the steam jacket that enters nozzle 5 after Venturi 7 mixing, the temperature in A district is 100 ℃, and gauge pressure is 0.05MPa; B district temperature is 110 ℃, and gauge pressure is 0.05MPa.
From carrying the hot water that dense device 6 extracts out is 30 liters/hour, and the hot water pump rate of discharge is 75 liters/hour, from the solvent quality content that exports 8 effusive micelles less than 1% (butt).
Claims (8)
1. the steam stripping coacervation and separation device of a polymers soln, it is characterized in that comprising have import and polymer beads water out and about be divided into the horizontal knockouts in A district and B district, be installed in the agitator in A district and B district respectively, be installed in three fluid tips of horizontal knockouts import, be connected the polymers soln pipeline on three fluid tips, be connected the B district rising gas pipeline above the horizontal knockouts B district, the venturi mixer that is connected with other heating steam pipeline with rising gas pipeline, be connected the B district heating steam pipeline of bottom, horizontal knockouts B district, be connected the A district rising gas pipeline above the horizontal knockouts A district, be connected the condenser on the A district rising gas pipeline, be undertaken on the separation sieve below the polymer beads water out, be connected the hot-water cylinder below the separation sieve, be installed in the dense device of carrying below the horizontal knockouts A district, with carry the dense water pipeline of carrying that dense device is connected, be connected the hot water pump of carrying on the dense water pipeline, be connected to circulating hot water pipeline and hot water line between hot water pump and polymers soln pipeline and the horizontal knockouts A district, hot water line, the circulating hot water pipeline is installed with the hot water flow meter respectively with carrying on the dense water pipeline, circulating hot water under meter and carry concentrated stream amount meter, hot-water cylinder and carrying between the dense water pipeline with pipeline connects, and venturi mixer also is connected with the chuck of pipeline with three fluid tips.
2. according to the steam stripping coacervation and separation device of the described polymers soln of claim 1, it is characterized in that said two agitators are all near the eccentric installation of central dividing plate.
3. according to the steam stripping coacervation and separation device of claim 1 or 2 described polymers solns, it is characterized in that said two agitators are axial flow type.
4. according to the steam stripping coacervation and separation device of the described polymers soln of claim 1, it is characterized in that three fluid tips are made up of static mixer and steam jacket, polymers soln and circulating hot water mix in static mixer, by in the chuck from the water vapor preheating of venturi mixer, the three sprays into the A district of knockouts together then, static mixer has 5～20 mixed cells, and the hot water volumetric flow rate that enters nozzle is 0.1～2.0 times of polymers soln volumetric flow rate.
5. according to the steam stripping coacervation and separation device of the described polymers soln of claim 1, it is characterized in that having out at the lower partition of horizontal stirring knockouts, the size that flashboard moving up and down is used for regulating perforate is equipped with in this perforate, and connecting one on this flashboard has the gland sealed screw rod that flashboard can be moved up and down at wall.
6. according to the steam stripping coacervation and separation device of the described polymers soln of claim 1, it is characterized in that in order to save energy, the rising steam in pyritous B district is used for heating the A district, for the pressure that prevents to cause thus the B district raises, the rising steam of setting up a venturi mixer attraction B district on A district heating steam pipeline enters the A district and does not increase the pressure in B district.
7. according to the steam stripping coacervation and separation device of the described polymers soln of claim 1, it is characterized in that saidly carrying dense device by the bigger cylindrical metal silk screen of diameter with support the wire cylinder mould that its metal cage is formed, the mesh of wire cloth is less than 4 * 4mm.Blowback steam or the nitrogen mouth that prevents that micelle from stopping up is equipped with in the bottom of wire cylinder mould, and blowback can be regularly or not timing, also can be pulsed.
8. polymers soln separation method that utilizes the steam stripping coacervation and separation device of the described polymers soln of claim 1～7, the mass concentration that it is characterized in that said polymers soln is 5～80%, the temperature in horizontal knockouts A district is that 70～100 ℃, gauge pressure are 0.01～0.05MPa, B district temperature is that 90～110 ℃, gauge pressure are 0.01～0.05MPa, and the hot water volumetric flow rate that enters horizontal knockouts is 2～15 with the ratio of polymers soln volumetric flow rate.
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| CN101235105B (en) * | 2007-12-30 | 2010-06-23 | 中国石油大庆石油化工总厂 | Method for agglomerating solution-polymerized rubber |
| CN101565471B (en) * | 2009-05-22 | 2010-11-10 | 孙建军 | Energy-saving method of synthetic rubber technique and equipment thereof |
| CN102234356A (en) * | 2010-04-30 | 2011-11-09 | 青岛伊科思新材料股份有限公司 | Method for producing rare-earth isoprene butadiene rubber |
| CN107793504A (en) * | 2016-09-06 | 2018-03-13 | 中国石油化工股份有限公司 | A kind of device of rubber polymer cohesion |
| CN107793498A (en) * | 2016-09-06 | 2018-03-13 | 中国石油化工股份有限公司 | A kind of method and apparatus of rubber polymer cohesion |
| CN109776853A (en) * | 2017-11-10 | 2019-05-21 | 中国石油化工股份有限公司 | Method for recovering solvents for ethylene/alpha-olefin technique for producing elastomer |
| CN109776855A (en) * | 2017-11-10 | 2019-05-21 | 中国石油化工股份有限公司 | Method for recovering solvents for rare-earth isoprene rubber production technology |
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| FR2749310B1 (en) * | 1996-06-03 | 1998-08-14 | Atochem Elf Sa | PROCESS FOR PRODUCING COAGULATED POLYMER LATEX PARTICLES |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101235105B (en) * | 2007-12-30 | 2010-06-23 | 中国石油大庆石油化工总厂 | Method for agglomerating solution-polymerized rubber |
| CN101565471B (en) * | 2009-05-22 | 2010-11-10 | 孙建军 | Energy-saving method of synthetic rubber technique and equipment thereof |
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| CN102234356B (en) * | 2010-04-30 | 2013-03-06 | 青岛伊科思新材料股份有限公司 | Method for producing rare-earth isoprene butadiene rubber |
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| CN107793498A (en) * | 2016-09-06 | 2018-03-13 | 中国石油化工股份有限公司 | A kind of method and apparatus of rubber polymer cohesion |
| CN107793504B (en) * | 2016-09-06 | 2019-09-27 | 中国石油化工股份有限公司 | A kind of device of rubber polymer cohesion |
| CN107793498B (en) * | 2016-09-06 | 2019-11-12 | 中国石油化工股份有限公司 | A kind of method and apparatus of rubber polymer cohesion |
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| CN109776855A (en) * | 2017-11-10 | 2019-05-21 | 中国石油化工股份有限公司 | Method for recovering solvents for rare-earth isoprene rubber production technology |
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