CN1243028C - Method and apparatus for continuous polymerization of polymer - Google Patents
Method and apparatus for continuous polymerization of polymer Download PDFInfo
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- CN1243028C CN1243028C CN 03121562 CN03121562A CN1243028C CN 1243028 C CN1243028 C CN 1243028C CN 03121562 CN03121562 CN 03121562 CN 03121562 A CN03121562 A CN 03121562A CN 1243028 C CN1243028 C CN 1243028C
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Abstract
To provide a method of polymerization of a polymer, by which the accurate component concentration of each monomer component including a monomer component of nonpolymerization reaction recovered by a monomer recovery process in a monomer adjusting part is automatically and continuously controlled and a polymerization equipment therefor. Unreacted monomer components of polymerization occurring in the polymerization of two or more component-based monomers are recovered by a monomer adjusting tank (3) and the recovered monomer components are continuously returned to the monomer adjusting tank (3). The flow rate and the component concentration of the recovered monomer component returned to the monomer adjusting tank (3) are measured. The feed flow rate of each component monomer fed to the monomer adjusting tank (3) is automatically controlled based on the measured results and the composition concentration of a polymer formed in a polymerization reactor (4) is made constant.
Description
Technical field
The present invention is supplied in a kind of continuous polymerization method and the polymerization unit thereof of various polymkeric substance of the monomeric feed rate of each raw material (virgin) of monomer modulation portion with stepless control about the yield according to two or more polymerization unreacted monomer (monomer) composition.
Background technology
General polymerization thing (polymer) is to make the polymerization and getting in addition of two or more monomer components.For example, ABS resin is to make the polymerization and getting in addition of vinyl cyanide (acrylonitrile), divinyl (butadiene), vinylbenzene (styrene), the MBS resin is the polymkeric substance of methyl methacrylate (methylmethacrytate), divinyl (butadiene), vinylbenzene (styrene), and acrylic copolymer (copolymer) is to make polymerization and getting in addition such as vinyl cyanide, vinyl acetate (vinyl acetate), methyl acrylate (acrylic methyl).
For example, the acrylonitrile copolymer that becomes the spinning material of acrylic fiber (acrylic fiber) be make acrylonitrile monemer and can with the nonionic comonomer (comonomer) of the acrylate (acrylic ester) of its copolymerization, methacrylic ester (methacrylate), vinyl acetate, acrylamide (acrylamide) etc. by radical polymerization (free-radicalpolymerization) manufacturing.With the acrylonitrile copolymer is the spin processes of raw material, makes acrylic copolymer through being dissolved in organic solvent, or the dissolution process of inorganic solvent, and by the wet type spin processes, dry spinning method or half dry type spin processes make fiber (staple) or filament (filament).
The manufacturing employing of acrylonitrile copolymer is that the continuous suspension polymerization mode of reaction media is more with water.In this continuous suspension polymerization mode, with indivedual metering vinyl cyanide and comonomer, be supplied in the monomer preparation vessel by raw material tank (tank) and MONOMER RECOVERY operation.Adjust monomer in the groove and put into the copolymerization of being made up of the polymkeric substance of making and forms, consideration vinyl cyanide and copolymerization be with monomeric reactive ratio, must be tight be set in certain value.
Polymeric kettle is by the synthetic vinyl cyanide of constituent concentration, comonomer, water, catalyst etc. together, adds polymerization starter (polymerization initiator) and carries out polymerization.The polymerization starter of this moment generally is to use the initiator of mineral-type.The mineral-type initiator is for example in the majority with the combination of the oxidation-reduction system that uses ammonium persulphate (ammonium persulfate)-sodium bisulfite (sodium bisulfite)-ferrous sulfate (ferroussulfate), containing above-mentioned comonomer is the monomer component of principal constituent with the vinyl cyanide, when the sulfuric acid water that has a reaction media effect when use begins polyreaction, form the particle shaped polymer of tens of microns (μ), with the state of aqueous liquid dispersion, can get the vinyl cyanide polymkeric substance.
The polymer system that takes out from polymeric kettle adds short-stopper with stopped reaction.Make the short-stopper of the occasion of vinyl cyanide polymkeric substance with water system suspension polymerization, must keep making the acidic aqueous solution neutral function of reactive system, use sodium oxalate (sodium oxalate), the aqueous electrolyte liquid of sodium bicarbonate (sodium bicarbonate), disodium EDTA etc.Again, forbid the monomer polymerization of vinyl cyanide in storing or in the transportation, for example add the resistance polymerizing agent of p methoxy phenol (p-methoxyphenol) etc. usually at starting monomer in advance.
The short-stopper of polyreaction as usually when the vinyl cyanide polymkeric substance is made in water system suspension polymerization mode employed short-stopper can not become problem.After aqueous solutions of polymers adds short-stopper, carry out the recovery of unreacted monomer.The recovery method of polymerization unreacted monomer composition, distillation tower in the separated part of polymkeric substance and polymerization unreacted monomer composition, make after the aqueous solutions of polymers straight run distillation, make gasification isolating unreacted monomer composition and water deliver to distiller (condenser) and condense and become the solution of monomers/water.This solution is to be separated into monomer component and water by decanting vessel (decanter).Isolating polymerization unreacted monomer composition is recovered through Jie's monomer preparation vessel and returns in polymerization reaction kettle.On the one hand, the moisture that remains in the polymkeric substance is to be removed by common drying mode.Previous as above-mentioned method reclaims polymerization unreacted monomer composition, modulates the operation that becomes normality at the monomer preparation vessel, handles with batch (batch).
So, make when reclaiming operation that the polymerization unreacted component sends the monomer preparation vessel back to, need to measure in advance the constituent concentration of the polymerization unreacted monomer composition when sending the monomer preparation vessel back to batch processing.Usually, this measures the compositional analysis from polymerization unreacted monomer composition, and the modulation of the monomer in the monomer preparation vessel is carried out after being in the majority.From its measurement result, the next polymerization unreacted monomer of sending the monomer preparation vessel back to decision becomes the flow of component.The most personnel of this kind operation and managerial demand are not only taken its long-time, inevitable one-tenth component and can be produced dispensing error.More and, because of the relation of batch processed, the storage tanks than required above recovery monomer component must be set.
Summary of the invention
The invention provides a kind of polymerization process of polymkeric substance and polymerization unit solving above-mentioned problem, concrete purpose is included in the not polyreaction that the MONOMER RECOVERY operation reclaimed with automatic and successive control monomer component is at the correct constituent concentration of interior each monomer component in the monomer modulation portion.
Above-mentioned purpose is made by each monomer more than the binary by the monomer modulation portion of first basic structure of the present invention forms the synthetic monomer mixed solution of concentration institute in polyreaction portion polymeric successive polymerization operation in addition, possessing the polymerization unreacted monomer composition that makes polyreaction portion reclaims continuously, send back to continuously in the monomer modulation portion with the polymerization unreacted monomer composition that makes recovery and to constitute, it is characterized in that, comprise measuring and send back in the flow and the constituent concentration of the polymerization unreacted monomer composition of monomer modulation portion, and according to its measurement result, for the composition concentration that makes the polymkeric substance of deriving from polyreaction portion keeps certain, control is supplied in the continuous polymerization method of polymkeric substance of the monomeric supply flow rate of each composition of above-mentioned monomer modulation portion and is reached.
Can be suitable for being implemented about continuous polymerization method by the continuous polymerization device that possesses second basic structure of the present invention again.The basic structure of this continuous polymerization device, it is characterized in that, comprise, the different monomer reservoir that binary is above, the monomer modulation portion, polyreaction portion, the polymkeric substance separated part of isolating polymer and polymerization unreacted monomer composition, and the recoverer of polymerization unreacted monomer composition, each one links with a plurality of pipelines, comprise first determination part and control part, wherein, flow and each constituent concentration of the polymerization unreacted monomer composition first determination part is measured from the recoverer of above-mentioned polymerization unreacted monomer composition to the pipeline of sending polymerization unreacted monomer composition back to of above-mentioned monomer modulation portion, control part is according to the measurement result by first determination part, calculate the flow that is supplied in each monomer component of monomer modulation portion from the monomer reservoir, and control these supply flow rates.
According to the present invention with aforementioned basic structure, recoverer at polymerization unreacted monomer composition is sent in the way of monomer modulation portion the polymerization unreacted monomer composition of recovery, measure its supply flow rate by first determination part, extract the constituent concentration that its part is determined at recovery monomer component contained in the fluid simultaneously out.At this moment, the preferred polymkeric substance of sending from polyreaction portion with second determination part and the 3rd determination part mensuration is simultaneously formed the constituent concentration of the polymerization unreacted monomer concentration and/or the polymer fluid.When these determination datas are sent to control part, for the composition concentration that makes the polymkeric substance of being sent from polyreaction portion keeps certain, at the supply flow rate of first determination part according to the data decision polymerization unreacted monomer composition of measuring, determine the supply flow rate of the starting monomer that will supply with from each reservoir of starting monomer simultaneously, be sent to the flow control division of each one according to the signal of these decisions, automatically the flow of each monomer component of sending from each one of control.Again, also can get rid of above-mentioned second determination part, be input into control part with the normal data that makes polymkeric substance composition and polymerization unreacted monomer constituent concentration in advance.This kind occasion, by the data that the more above-mentioned normal data and first determination part are measured, also may command is from the monomer feed rate of each one.
Preferably measure flow and the constituent concentration of supplying with the monomer component of polyreaction portion from above-mentioned monomer modulation portion more again in the present invention.Therefore, expect to possess more again the 4th determination part and be determined at the flow of the monomer mixed solution that pipeline circulated that links above-mentioned monomer modulation portion and polyreaction portion and the constituent concentration of each monomer component.Supply with each an amount of raw material (virgin) monomer in the monomer modulation portion as stating, simultaneously as above-mentioned to send into the polymerization unreacted monomer of recovery in right amount from each reservoir of the starting monomer of binary system.The monomer modulation portion makes with each monomer import volume of suitable adjustment and sends polyreaction portion to next operation continuously.
At this moment, be the constituent concentration of measuring each monomer component of sending from the monomer modulation portion by the 3rd determination part in the present invention, whether to confirm constituent concentration at defined.In its constituent concentration and the different occasion of predefined concentration, control part calculates it and surpasses or insufficient component, signal is delivered to corresponding monomer supply unit, to control the monomer import volume of each monomer supply unit.
By continuous polymerization method of the present invention institute polymeric polymkeric substance, have with the monomer more than the above-mentioned binary of typical example, be principal constituent with the vinyl cyanide, the multipolymer of the vinyl cyanide of the polymkeric substance of the comonomer of copolymerization therewith.Other example is for there being the MBS resin that makes vinyl cyanide, divinyl, vinylbenzene institute polymeric ABS resin or methyl methacrylate, divinyl, cinnamic polymkeric substance.
Has gas chromatograph (gas chromatograph) in said determination portion, thus the flow of each one of gas chromatograph for determination and constituent concentration or composition concentration.Using the occasion of gas chromatograph, can make gas chromatograph and control part in succession, delivering to control part immediately by making its determination data in the mode of electricity.More and by establishing the time difference at minute, can contain by single gas chromatograph and cover first～the 4th determination part, do not need to be provided with unnecessary determining instrument.
Description of drawings
Fig. 1 has the process picture sheet of paradigmatic system of the vinyl cyanide polymkeric substance of MONOMER RECOVERY device of the present invention for expression.
Fig. 2 is the square frame line chart of the stepless control flow process of the polymerization process that the is illustrated in representative embodiment of the present invention monomer feed rate that is directed in the monomer modulation portion.
Fig. 3 is directed in the square frame line chart of stepless control flow process of the monomer feed rate of monomer modulation portion for expression other example of the present invention.
1: the storage tanks of vinyl cyanide
2a, 2b: volume pump
3: the monomer preparation vessel
4: polymerization reaction kettle
5: distillation tower
6: distiller
7: decanting vessel
8: reclaim the monomer groove
9: gas chromatograph
10: control part
Embodiment
Below, make representative example of the present invention according to graphic detailed description the in detail.
Though below illustrated example be to make continuous polymerization method of the present invention and polymerization unit be applicable to that vinyl cyanide polymerization technique by water system suspension polymerization mode, the present invention are not to be defined in the example of the following stated and applicable to multiple polymerization technique.
Fig. 1 is the successive polymerization that makes according to this example.Whole modes with pattern of recovery process are represented.At first, from the storage tanks 1 of the vinyl cyanide of main raw material through Jie's volume pump (pump) 2a to monomer preparation vessel 3, the one side metering is to drop into institute quantitatively.At this example, be to make the p methoxy phenol that in storage, does not play polymerization and add the resistance polymerizing agent with weight ratio 40ppm at above-mentioned storage tanks 1 stored vinyl cyanide.The resistance polymerizing agent except aforesaid right-methoxyl group phenol, can use Resorcinol (hydroguinone), to the bitter vinegar hydrazine (diphenyl picrylhydrazyl) of t-butyl catechol (p-t-butylcatechol), hexichol, benzoquinones (benzoquinone), galvinoxyl, 1,3,5-triphenylfeldazyl etc.
At above-mentioned monomer preparation vessel 3 comonomer with second composition of copolymerization of acrylonitrile is arranged more again, never second storage tanks of icon with same one side metering one side with fixed ratio input, the unreacted polymerization unreacted monomer composition of being sent from polymerization reaction kettle 4 is sent into through recovery when polymerization simultaneously.Adjust 3 synthetic sticking accent stock liquids of groove at monomer and send into polymerization reaction kettle 4 continuously through next the volume pump 26 of being situated between.Pure water in these polymerization reaction kettle 4 other necessary amounts of supply adds polymerization starter or various auxiliary agent simultaneously.
Use mineral-type redoxomorphism (redox) initiator at polymerization starter of the present invention.Mineral-type redoxomorphism initiator can be selected among common oxygenant, reductive agent.Occasion by the redoxomorphism that combination constituted of oxygenant and reductive agent, its representative, the normally used ammonium persulphate of oxygenant (ammonium persulfate), Potassium Persulphate (potassiumpersulfate), Sodium Persulfate (sodium persufate) etc., the normally used S-WAT of reductive agent (sodium sulfite), ammonium sulphite (ammonium sulfite), sodium bisulfite (sodiumhydrogen sulfite), ammonium bisulfite (ammonium hydrogen sulfite), Sulfothiorine (sodium thiosulfate), ammonium thiosulfate (ammonium thiosulfate), V-Brite B (sodium dithionite), sodium sulfoxylate formaldehyde (sodium formaldehydesulfoxylate), left-handed vitamin C (L-ascorbic acid), glucose (dextrose) etc.The compound that ferrous sulfate also capable of being combined or copper sulfate (cupric sulfate) etc. use uses.Wherein, preferably with the combination of ammonium persulfate-sodium bisulfite (ammonium)-ferrous sulfate.Though any ratio of the ratio of reductive agent and oxygenant all can, with efficient when carrying out polymerization the equivalence ratio of reductive agent and oxygenant be advisable with 1～4.
The vinyl cyanide polymkeric substance of the repeating unit that beyond the employed vinyl cyanide polymkeric substance of this example is acrylonitrile monemer, also can be constituted by monoene (monoolefin) property monomer with its energy copolymerization.At this vinyl cyanide polymkeric substance by being constituted by the acrylonitrile monemer of at least 60 weight %.The amount of acrylonitrile monemer is during less than 60 weight %, and the vinyl cyanide synthon can not keep original all fiber functions.For example can lift vinylformic acid (acrylic acid) at this copolymerizable monoene monomer, methacrylic acid (methacrylic acid) and ester (ester) thereof, acrylamide (acrylamide), vinyl acetate (vinyl acetate), vinylbenzene (styrene), vinylchlorid (vinyl chrorite), ethylene chloride fork (vinylidene chloride), MALEIC ANHYDRIDE (maleic anhydride), N-replaces maleic two vinegar imines (maleinimide), divinyl (butadien), isoprene (isoprene) etc.Also can use sulphur vinegar methallyl ethers (p-sulfonylmethallyl ether), methallyl sulfonic acid (methallyl sulfonic acid), propenyl sulfonic acid (allyl sulfonic acid), styrene sulfonic acid (styrene sulfonic acid), 2-acrylamide-2-methyl propane sulfonic acid (2-acrylamide-2-methylpropan sulfonicacid), 2-thio-ethyl acrylate (2-sulfo ethyl methacrylate) and these salt and be copolymerizable monomer again.
The monomeric polymerization of vinyl cyanide is to be undertaken by following condition.That is, polymeric reaction temperature preferably is made as 30～80 ℃.The vinyl cyanide evaporation was and discrete outside reactive system when polymerization temperature surpassed 80 ℃, and polymerisation conversion reduces.Polymerization velocity reduces during again less than 30 ℃, and not only turnout reduces, and the polymerization stability can be impaired.Aggregated media is so that water or ion exchanged water are advisable.More and to the ratio of monomeric ion exchanged water (below, be called water/monomer than) though can be any ratio, preferably with water/monomer than the scope that is 1.0～5.0.Monomeric average retention time in polymerization reaction kettle just can for make the common time of being adopted when the vinyl cyanide polymkeric substance is made in water system suspension polymerization mode.Hydrogen ion concentration in polymerization reaction kettle is to get final product can play redox scope rapidly at employed catalyst, is preferably the acid field of pH2.0～3.5.
Add short-stopper with stopped reaction at the polymkeric substance that is taken out from polymerization reaction kettle 4.Polyreaction stop agent so long as when common vinyl cyanide polymkeric substance is made in water system suspension polymerization mode the short-stopper that used do not limit.After aqueous solutions of polymers adds short-stopper, carry out the recovery of unreacted monomer.The recovery method of polymerization unreacted monomer can adopt the method that makes the aqueous solutions of polymers straight run distillation or in case dehydration makes unreacted monomer separate two modes of back distillatory method with polymkeric substance.Adopt the method that makes the aqueous solutions of polymers straight run distillation at this example.At this example, at 4 polymeric aqueous solutions of polymers of polymerization reaction kettle as shown in Figure 1, take out and importing distillation tower 5 from polymerization reaction kettle 4.
At distillation tower 5, isolating polymer and monomers/water, simultaneously the mixed solution of monomers/water is in distillation tower 5 distillations and gasify, and is directed in distiller 6 and condenses and become the mixed solution of unreacted monomer component of polymerization and water.Polymerization unreacted monomer composition in distiller 6 liquefaction is separated through Jie's inclinator 7 with the mixed solution of water, and water is sent distillation tower 5 back to.As both stating, a side monomer component reclaims the monomer groove through being situated between and sends monomer preparation vessel 3 back to.
The mensuration that Fig. 2 extracts out at two above inter processes of successive polymerization operation according to this example for the expression square frame line chart in the extraction place of monomer component.
At this example, the extraction of reclaiming monomer component is delivered to the way of monomer preparation vessel 3 and is carried out from reclaiming monomer groove 8, from monomer preparation vessel 3 is sent into the way of polymerization reaction kettle 4, extract monomer component out, more and by the polymer fluid of sending to distillation tower from polymerization reaction kettle 4 extract polymerization unreacted monomer composition out.The mixed stream of the unreacted monomer composition/water in the polymer fluid of this extraction is delivered to gas chromatograph 9.The constituent concentration of the sample of extracting out at this example and the composition concentration of polymkeric substance be by gas chromatograph with instantaneous assay determination in addition, these data determination signal is delivered to control part 10.
Mensuration in constituent concentration of the present invention or composition concentration is not to be defined in gas chromatograph 9, for example can use liquid chromatograph yet.So in the occasion of using gas chromatograph 9, sending into the polymerization unreacted monomer composition of monomer preparation vessel 3 through recovery, deliver to the monomer mixed solution of polymerization reaction kettle 4 from monomer preparation vessel 3, and the sample of the mixed stream of the polymer/polymeric unreacted monomer composition/water of deriving from polymerization reaction kettle 4 extracts out when establishing the time difference with mensuration, can carry out every mensuration by single gas chromatograph 9.That is, do not need to establish individually first～the 4th determination part.At this example,, detect and flow in the interior fluidic flow of each pipe arrangement that each sample is extracted out with mensuration constituent concentration or composition concentration while again.
So, be converted to numerary signal about constituent concentration, composition concentration and the data on flows of being measured and deliver to control part 10.Calculate each weight at each monomer component of each sample extraction unit at control part 10 according to these data, the composition weight of polymkeric substance etc. are also compared, to judge these accordances of every.Again, the also ratio of components of each monomeric composition ratio of components of computing or polymkeric substance etc. simultaneously.These operation results and predefined constituent concentration and composition concentration ratio are.To judge its accordance.The occasion of not having above-mentioned accordance is adjusted polymerizing condition, or the monomer supply flow rate of the monomer supply unit more than the control binary, and the monomeric supply flow rate of the unreacted recovery of controlled polymerization is to guarantee above-mentioned accordance.
More and at this example also can prepare to have the desired constituent concentration of monomer component and the reference liquid of composition concentration in addition, this reference liquid imports gas chromatograph, when measuring, the data signal of its constituent concentration is delivered to control part 10, at control part 10 relatively this normal data and each determination data, with adjust according to the constituent concentration of each determination data or form concentration surpass or in shortage, controlled the supply flow rate of each monomer component.
Fig. 3 represents other example of the present invention.According to this example, the unreacted recovery monomer component of polymerization of sending monomer adjustment groove 3 back to is not carried out special flow adjustment, the flow of foundation recovery monomer component and the variation of constituent concentration are with the feed rate of the supply unit of successive control starting monomer.
That is, same with above-mentioned example, the first monomer component A and the second monomer component B of starting raw material that is suitable for the use level of polymerization velocity mixes to devote monomer preparation vessel 3 continuously with the unreacted recovery monomer component of polymerization.Extract out the way of its supply from a part that reclaims the unreacted recovery monomer component of polymerization that monomer groove 8 supplied with, deliver to gas chromatograph 9, measure its concentration composition.Measure the supply flow rate that reclaims monomer component simultaneously.Its flow is to deliver to control part 10 one by one with the determination data of the constituent concentration of being measured with gas chromatograph 9.
In control part 10 input about each constituent concentration of the constituent concentration of the first monomer component A in the modulating liquid that sets in advance and the second monomer component B and devote the various data of full input flow of the monomer component of monomer preparation vessel 3, in the said determination data that at every moment change of control part 10 according to these data, to calculate to first monomer component A of monomer preparation vessel 3 and the input flow of the second monomer component B, signal is delivered at the supply unit configuration of the first monomer component A and the second monomer component B volume pump without icon, to increase and decrease each the monomer component A that is discharged from these pumps, the delivery flow of B is controlled the above-mentioned input flow of being calculated.
Secondly, make the present invention according to the embodiment of the polymerization process that is applicable to the vinyl cyanide polymkeric substance to be illustrated more specifically.
Embodiment 1:
Successive polymerization at vinyl cyanide and vinyl acetate, the vinyl cyanide and the vinyl acetate of starting monomer are devoted the monomer preparation vessel, import the unreacted recovery monomer of polymerization of vinyl cyanide and vinyl acetate mixed solution simultaneously with the flow of 5.8t/hr, to carry out monomeric continuous modulation.At this moment, the overall supplies of the modulating liquid of supplying with from the monomer preparation vessel to polymerization reaction kettle is 16.0t/hr, make vinyl acetate in the modulating liquid be set in any concentration of 5%～15% (weight ratio) scope, polymerization unreacted by series connection (inline) gas chromatograph gained reclaims monomeric vinyl acetate concentration, and the necessary flow of calculating the vinyl cyanide of initiate starting monomer and vinyl acetate is to modulate continuously.Monomeric vinyl acetate concentration after the modulation of gained in 0.05%, can obtain the modulating liquid that sets to the error of purpose concentration continuously.
Claims (9)
1. the continuous polymerization method of a polymkeric substance makes by the monomeric synthetic monomer mixed solution of concentration of forming more than two compositions in the monomer modulation portion, and in polyreaction portion polymeric successive polymerization operation in addition, its formation has:
Reclaim the polymerization unreacted monomer composition of polyreaction portion continuously, make the polymerization unreacted monomer composition of recovery send the monomer modulation portion continuously back to, it is characterized in that, comprising:
Flow and constituent concentration to the polymerization unreacted monomer composition of sending the monomer adjustment part back to are measured; And
According to its measurement result, for the composition concentration that makes the polymkeric substance of being derived from polyreaction portion keeps certain, control is supplied in the monomeric supply flow rate of each composition of monomer modulation portion.
2. continuous polymerization method as claimed in claim 1 is characterized in that, comprises the composition concentration of the polymkeric substance that mensuration is derived from polyreaction portion.
3. continuous polymerization method as claimed in claim 1 is characterized in that, comprises mensuration from flow and the constituent concentration of monomer modulation portion to the monomer component of polyreaction portion supply.
4. as one of them the described continuous polymerization method in the claim 1 to 3, it is characterized in that the above monomer of aforementioned two compositions is a principal constituent with the vinyl cyanide, and comprise the comonomer with copolymerization of acrylonitrile.
5. the continuous polymerization device of a polymkeric substance, comprise different monomer reservoir, monomer modulation portion, polyreaction portion, polymerization separated part and recoverer that two compositions are above, the polymerization separated part is isolating polymer and polymerization unreacted monomer composition, recoverer is for reclaiming polymerization unreacted monomer composition, aforementioned each one is linked by a plurality of pipelines, it is characterized in that, comprise:
First determination part is measured from the recoverer of aforementioned polymerization unreacted monomer composition and is sent flow and each constituent concentration of the polymerization unreacted monomer composition the pipeline of polymerization unreacted monomer composition back to the aforementioned monomer adjustment part; And
Control part according to the measurement result of aforementioned first determination part, is calculated from the flow of monomer reservoir to each monomer component of monomer modulation portion supply, with the control supply flow rate.
6. continuous polymerization device as claimed in claim 5 is characterized in that, also comprises second determination part, measures the composition concentration of the polymkeric substance that is circulated from the derivation pipeline of aforementioned polyreaction portion.
7. continuous polymerization device as claimed in claim 5 is characterized in that, also comprises the 3rd determination part, and the polymer fluid that is circulated by the derivation pipeline from aforementioned polyreaction portion is to measure polymerization unreacted monomer constituent concentration.
8. continuous polymerization device as claimed in claim 5 is characterized in that, also comprises the 4th determination part, is determined at the flow of the monomer mixed solution that pipeline circulated that links aforementioned monomer modulation portion and aforementioned polyreaction portion and the constituent concentration of each monomer component.
9. as one of them the described continuous polymerization device in the claim 6 to 8, it is characterized in that aforementioned determination part comprises gas chromatograph.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002102136A JP3954887B2 (en) | 2002-04-04 | 2002-04-04 | Polymer continuous polymerization method and polymerization equipment |
| JP2002102136 | 2002-04-04 |
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| CN1448412A CN1448412A (en) | 2003-10-15 |
| CN1243028C true CN1243028C (en) | 2006-02-22 |
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| JP5631550B2 (en) * | 2009-02-27 | 2014-11-26 | 丸善石油化学株式会社 | Method for producing copolymer for photoresist |
| CN101864017B (en) * | 2009-04-15 | 2012-05-30 | 中国石油天然气股份有限公司 | Automatic control method of butadiene polymerization |
| CN102464735B (en) * | 2010-11-19 | 2014-01-08 | 中国石油化工股份有限公司 | Device for producing polypropylene by intermittent liquid phase bulk polymerization method and method |
| CN102464752B (en) * | 2010-11-19 | 2014-04-02 | 中国石油化工股份有限公司 | Device for producing ethylene random copolymerization polypropylene by intermittent liquid phase bulk polymerization method and method |
| CN103030727B (en) * | 2011-09-30 | 2015-03-11 | 中国石油化工股份有限公司 | Apparatus and method for production of ethylene polypropylene random copolymers by batch liquid-phase bulk technique |
| CN103030725B (en) * | 2011-09-30 | 2015-03-11 | 中国石油化工股份有限公司 | Apparatus and method for production of alpha-olefin polypropylene random copolymers by batch liquid-phase bulk technique |
| CN103387624B (en) * | 2012-05-07 | 2015-06-17 | 中国石油化工股份有限公司 | Preparation method of olefin polymer |
| CN109705252B (en) * | 2017-10-25 | 2021-02-05 | 中国石油化工股份有限公司 | System for ionomer production, production method and applications thereof |
| CN109655547A (en) * | 2018-12-29 | 2019-04-19 | 山东玉皇化工有限公司 | A kind of device and method of gas chromatograph detection exhaust gas component and real-time traffic |
| CN116078335B (en) * | 2023-04-11 | 2023-07-21 | 长盛(廊坊)科技有限公司 | Device and method for stably recycling monomer concentration |
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| JPS53139691A (en) * | 1977-05-11 | 1978-12-06 | Mitsubishi Rayon Co Ltd | Preparation of acrylonitrile polymer solution |
| JPS6411112A (en) * | 1987-07-02 | 1989-01-13 | Hitachi Chemical Co Ltd | Production of vinyl acetate-acrylic copolymer |
| JPH11116616A (en) * | 1997-10-20 | 1999-04-27 | Toray Ind Inc | Recovery of unreacted monomer and recovering apparatus |
| JP2000336115A (en) * | 1999-05-28 | 2000-12-05 | Toray Ind Inc | Production of vinyl polymer |
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| JP2003292503A (en) | 2003-10-15 |
| CN1448412A (en) | 2003-10-15 |
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