CN209501640U - The continuous synthesis system of suspension type polyvinyl-chloride - Google Patents
The continuous synthesis system of suspension type polyvinyl-chloride Download PDFInfo
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Abstract
The utility model discloses a kind of continuous synthesis systems of suspension type polyvinyl-chloride, including micro- reaction system, micro- reaction system includes the microreactor of at least thtee-stage shiplock, the cross-sectional area of the microchannel of the microreactor is 0.1~1mm, the cross-sectional area that the microchannel of the microreactor of front end is connected on along material flow direction is less than the cross-sectional area of the microchannel for other microreactors behind of connecting, and polymerization reaction carries out in microreactor.The utility model has the advantages that: 1) can be realized the continuous production of polyvinyl chloride；2) product quality will not be adversely affected；3) system structure is simple, and only needing same unit device to be arranged in juxtaposition can reach scale mass production purpose, and production is easy to control, conducive to industrially promoting.
Description
Technical field
The utility model relates to a kind of Production of PVC system, especially a kind of suspension type polyvinyl-chloride production technology.
Background technique
Suspension type polyvinyl-chloride production technology refers to Liquid vinyl chloride in an aqueous medium, under dispersing agent protection, by stirring
The effect of mixing is separated into uniform and stable drop, and the decomposition of initiator by being dissolved in vinyl chloride monomer is radical initiation reaction.Polymerization is anti-
It should include the elementary reactions such as chain initiation, chain growth, chain tra nsfer and chain termination.
Polymerization reaction is carried out in polymeric kettle, and polymeric kettle is the capital equipment of production system, by steel autoclave body liner
Stainless steel or enamel are made, heat-transferring jacket or interior cold comb, reflux condenser equipped with blender and control temperature etc..Polymerization
Afterwards, gained Corvic slurry enters slurry tank, then is sent into stripper plant with mashing pump, removes remaining chloroethene in slurry
After alkene monomer, it is re-fed into drying system and removes moisture, obtain finished product Corvic.Divide when polymerization to guarantee that acquisition is defined
The resin of son amount and range of molecular weight distributions simultaneously prevents implode, it is necessary to control the temperature and pressure of polymerization process.The grain of resin
Degree and size distribution are then controlled by the selection of mixing speed and dispersing agent and dosage.Therefore to maintain ambient stable in polymeric kettle,
Batch Process mode can only be used, continuous charging easily causes implode to cause security risk.
Utility model content
For the continuous production for realizing polyvinyl chloride, the utility model, which provides a kind of suspension type polyvinyl-chloride and continuously synthesizes, is
System.
The technical scheme adopted by the utility model is the continuous synthesis system of suspension type polyvinyl-chloride, including micro- reaction system
System, micro- reaction system includes the microreactor of at least thtee-stage shiplock, the cross section of the microchannel of the microreactor
Product is 0.1~1mm, and the cross-sectional area that the microchannel of the microreactor of front end is connected on along material flow direction is less than string
It is associated in the cross-sectional area of the microchannel of microreactor thereafter, polymerization reaction carries out in microreactor.
Inventor has done many researchs about the continuous production technology of polyvinyl chloride in recent years, and early-stage study is all unsuccessfully to accuse
Eventually, reason is to be difficult to avoid that implode.The reason of implode occurs in continuous production may be that continuous feed leads to dispersing agent
It is difficult to realize the protection to monomer, causes to generate bulky grain polymer in polymerization process, monomer molecule is with bulky grain polymer
Center polymerize rapidly, and localized heat release excessively leads to implode.
Inventor proposes the reaction unit using microreactor alternative reaction kettle as polymerization reaction in the present invention, real
Verify it is bright implode can be effectively prevent in continuous production, and product quality will not be adversely affected, there is reality
Feasibility.Its reason may be that microreactor is made of several microchannels, and the size by controlling microchannel can
Effectively bulky grain polymer is prevented to generate, to prevent implode.
It should be noted that since microchannel is small-sized, mistake that monomer polymerize and flowed in microchannel
The granulation process of journey polyvinyl chloride is also constantly promoting, before the reaction the phase, needs to react to prevent bulky grain polymer from generating
Microchannel cross-section product is controlled in lesser range, but as the polymer beads of progress generation early period of polymerization reaction are constantly long
Greatly, it is easy to microchannel is blocked, therefore late phase reaction microchannel should have relatively bigger cross-sectional area in the reaction,
So segment design should be carried out microchannel, since polyvinyl chloride particles size turns with vinyl chloride monomer in reaction process
The raising of rate and increase, segmentation according to be vinyl chloride monomer different phase conversion ratio.Simultaneously according to polymerization reaction first
When phase and mid-term, reaction speed is fast, the effect of reaction later period slow-footed feature and the microchannel in differential responses stage,
Preferably based on the microchannel of the rate of change setting different length of vinyl chloride monomer conversion ratio.Therefore as this preferred reality
Microreactor is designed at least as to the mode of thtee-stage shiplock, the microchannel tool of every level-one microreactor with novel middle inventor
There are different cross-sectional area and length, specific size those skilled in the art can flow through microchannel according to actual production fluid
Conversion rate of vinyl chloride situation of change experiment in the process determines.Such as the utility model provides a kind of preferred embodiment: described micro- anti-
Answer system by sequentially connected level-one microreactor, second level microreactor, three-level microreactor composition；The level-one microreactor
Microchannel length be 1~5m, cross-sectional area be 0.1~0.5mm2；The microchannel of the second level microreactor is long
Degree is 4~10m, and cross-sectional area is 0.3~0.8mm2；The microchannel length of the three-level microreactor is 10~20m, horizontal
Sectional area is 0.3~0.8mm2。
For the stabilization of maintaining reaction temperature, corresponding heat-exchange system can be set, reaction temperature is controlled, is easy reason
Solution, the common all kinds of heat-exchange systems in this field can be used in heat-exchange system, such as circulation, specific arragement construction can roots
It is designed according to the structure of microreactor.Such as inventors herein propose a kind of preferred scheme in the present invention: this is practical
The reaction zone that novel microreactors at different levels may include air-tight chamber and be arranged in air-tight chamber, the reaction zone
It is provided at least one microchannel, and circulating water heat-exchanging system is set simultaneously, recirculated water or inertia can be used in heat transferring medium
Liquid, heat-exchange system include the heat transferring medium inlet tube being connected to the air-tight chamber of microreactors at different levels and heat transferring medium outlet
Pipe.In the equipment course of work, heat transferring medium enters the gas of microreactors at different levels by the heat transferring medium inlet tube of heat-exchange system
In close property chamber, indirect heat exchange occurs with the microchannel internal-response object of reaction zone, reaction temperature is controlled 35~80
DEG C, so that reaction carries out.
The invention also discloses a kind of Production of PVC methods, comprising the following steps:
A, it is each led into micro- reaction system using raw materials for production as fluid in certain flow ratio by feed system, it is former
Material is mixed after entering microchannel, and polymerization reaction carries out in microchannel, controls reaction temperature by heat-exchange system
Degree is 35~80 DEG C, and reaction pressure is 0.1~1.2Mpa, and the total time that material passes through microreactor microchannels at different levels is 10
~500s reaches and final stage microreactor is added in terminator after target conversion, obtains Corvic slurry；
B, gained Corvic slurry enters slurry tank, then is sent into stripper plant with mashing pump, removes residual in slurry
After the vinyl chloride monomer stayed, it is re-fed into drying system and removes moisture, obtain finished product Corvic.
As the further improvement of this method, for micro- reaction system by sequentially connected level-one microreactor, second level is micro-
Reactor, three-level microreactor composition；The microchannel length of the level-one microreactor is 1~5m, cross-sectional area 0.1
~0.5mm2；The microchannel length of the second level microreactor is 4~10m, and cross-sectional area is 0.3~0.8mm2；Described three
The microchannel length of grade microreactor is 10~20m, and cross-sectional area is 0.3~0.8mm2；And the second level microreactor
It is greater than the cross-sectional area of the microchannel of level-one microreactor with the cross-sectional area of the microchannel of three-level microreactor；One
Grade microreactor conversion rate of vinyl chloride control 13~17%, the control of second level microreactor conversion rate of vinyl chloride 45~55%,
Three-level microreactor conversion rate of vinyl chloride is controlled 82~88%.
The polymerization reaction carried out in microreactor is divided into three phases by the program, according to polymerization reaction prometaphase speed
Fastly, stage of the later period slow-footed feature by vinyl chloride conversion ratio lower than 45~55% divides the prometaphase into, higher than this conversion ratio
Stage divides the later period into, and is provided with different microchannel length.And it need to prevent bulky grain from polymerizeing early period according to polymerization reaction
Object is formed, the reaction middle and later periods need to prevent the growth of polymer partial size cause channel blockage by conversion rate of vinyl chloride 13~17% with
Under stage divide reaction early period into, and according to its feature devise the microchannel cross-sectional area different from middle and later periods early period and
Length.Readily comprehensible, how much above-mentioned conversion rate of vinyl chloride can be judged according to heat of reaction.
As the further improvement of this method, the raw materials for production include vinyl chloride monomer, deionized water, initiator, point
Powder；The initiator is 0.1 hour selected from half-life period, and organic peroxide class of the half life temperature less than or equal to 85 DEG C causes
Agent (such as: diisobutyryl peroxide, cumyl peroxyneodecanoate, dicetyl peroxydicarbonate two (3- methoxybutyl),
1.1.3.3- tetramethyl butyl new decanoate ester peroxide, the new enanthic acid isopropyl phenyl ester of peroxidating, peroxy dicarbonate mixing, peroxide
Change neodecanoic acid tert-pentyl ester) one of or any several mixture；The dispersing agent includes main dispersant and dispersion aids, master
Dispersing agent is selected from one of methylcellulose, methylhydroxypropylcellulose, hydroxyethyl cellulose, hydroxypropyl cellulose or any
Polyvinyl alcohol one of or any several mixture of several mixtures and alcoholysis degree 60~90%；Help dispersion
Agent is selected from polyvinyl alcohol one of or any several mixture of the alcoholysis degree 30~60%.About each raw material selection with
The prior art is not different, and is common knowledge, is not remake excessive explanation herein.
The beneficial effects of the utility model are: 1) can be realized the continuous production of polyvinyl chloride；It 2) will not be to product quality
It adversely affects；3) system structure is simple, and only needing same unit device to be arranged in juxtaposition can reach scale mass production purpose,
Produce it is easy to control, conducive to industrially promoting.
Detailed description of the invention
Fig. 1 is the Vinyl Chloride Production System equipment flowsheet of the utility model.
In the figure, it is marked as 1- feed system, the micro- reaction system of 2-, 201- level-one microreactor, 202- second level microreactor,
203- three-level microreactor, 2001- air-tight chamber, 2002- reaction zone, 3- slurry tank, 4- terminator basin, 5- heat exchange system
System, 501- heat transferring medium inlet tube, 502- heat transferring medium outlet.
Specific embodiment
The present invention will be further described with reference to the accompanying drawings and examples.
As shown in Figure 1, the continuous synthesis system of the suspension type polyvinyl-chloride of the utility model, including sequentially connected charging system
System 1, micro- reaction system 2 and slurry tank 3；Further include terminator basin 4 and heat-exchange system 5, the heat-exchange system 5 with it is at different levels micro- anti-
Device is answered to connect, the terminator basin 4 is connect with three-level microreactor 203.Micro- reaction system 2 is by sequentially connected level-one
Microreactor 201, second level microreactor 202, three-level microreactor 203 form；Microreactors at different levels include air-tight chamber
2001 and the reaction zone 2002 that is arranged in air-tight chamber 2001, it is micro- logical that the reaction zone 2002 is provided with several reactions
Road.The heat-exchange system 5 includes the heat transferring medium inlet tube 501 being connected to the air-tight chamber 2001 of each microreactor and heat exchange
Media outlet pipe 502.
Embodiment one:
The production of polyvinyl chloride is used for using above-mentioned apparatus according to the following steps:
Wherein the microchannel length of level-one microreactor described in above-mentioned apparatus 201 is 2m, and cross-sectional area is
0.2mm2；The microchannel length of the second level microreactor 202 is 6m, cross-sectional area 0.5mm2；The micro- reaction of three-level
The microchannel length of device 203 is 13m, cross-sectional area 0.5mm2。
(1) according to the flow proportional set, by vinyl chloride monomer, deionized water, dispersing agent, (main dispersant selects methyl
The mixture for the polyvinyl alcohol that hydroxypropyl cellulose and alcoholysis degree are 70% polyvinyl alcohol and alcoholysis degree is 82% helps dispersion
Agent selection alcoholysis degree 45% polyvinyl alcohol), initiator (diisobutyryl peroxide and (the 3- methoxyl group fourth of dicetyl peroxydicarbonate two
Ester)), pH adjusting agent (ammonium hydrogen carbonate) microchannel of level-one microreactor 201 is each led into as fluid, raw material enters anti-
It is mixed after answering microchannel, polymerization reaction carries out in microchannel, and the circulating hot water from heat-exchange system 5 enters airtight
Property chamber 2001 and microchannel in reactant carry out indirect heat exchange, control reaction temperature is 57 DEG C, and reaction pressure is
0.8Mpa；Conversion rate of vinyl chloride is 15.6% at the end of the micro- reaction of level-one, and reaction mixture goes successively to second level microreactor 202
It is reacted；Conversion rate of vinyl chloride is 50.3% at the end of the micro- reaction of second level, and reaction mixture goes successively to three-level microreactor
203 are reacted；By terminator (N, N- diethyl hydroxylamine and tert-butyl hydroxy when the micro- reaction conversion rate of vinyl chloride of three-level is 85%
Methyl phenyl ethers anisole) be added three-level microreactor 203 obtain PVC slurry.Reaction mass is total by microreactor microchannels at different levels
Time is 120s.
(2) enter slurry tank 4 from the PVC slurry that three-level microreactor 203 comes out, vinyl chloride gas enters in slurry tank 4
Recovery system, PVC slurry are then sent into stripping system by mashing pump and remove remaining vinyl chloride, are re-fed into drying system and remove water
Point, obtain finished product Corvic.Through examining Corvic particle diameter distribution width 1.31, molecular weight distributing index exists
1.58, quality index meets GB/T5761.
Embodiment two:
The production of polyvinyl chloride is used for using above-mentioned apparatus according to the following steps:
Wherein the microchannel length of level-one microreactor described in above-mentioned apparatus 201 is 1m, and cross-sectional area is
0.1mm2；The microchannel length of the second level microreactor 202 is 4m, cross-sectional area 0.3mm2；The micro- reaction of three-level
The microchannel length of device 203 is 10m, cross-sectional area 0.3mm2。
(1) according to the flow proportional set, by vinyl chloride monomer, deionized water, dispersing agent, (main dispersant selects methyl
The mixture for the polyvinyl alcohol that hydroxypropyl cellulose and alcoholysis degree are 70% polyvinyl alcohol and alcoholysis degree is 88% helps dispersion
Agent selection alcoholysis degree 45% polyvinyl alcohol), initiator (diisobutyryl peroxide and (the 3- methoxyl group fourth of dicetyl peroxydicarbonate two
Ester)), pH adjusting agent (ammonium hydrogen carbonate) microchannel of level-one microreactor 201 is each led into as fluid, raw material enters anti-
It is mixed after answering microchannel, polymerization reaction carries out in microchannel, and the circulating hot water from heat-exchange system 5 enters airtight
Property chamber 2001 and microchannel in reactant carry out indirect heat exchange, control reaction temperature is 80 DEG C, and reaction pressure is
0.8Mpa；Conversion rate of vinyl chloride is 15.3% at the end of the micro- reaction of level-one, and reaction mixture goes successively to second level microreactor 202
It is reacted；Conversion rate of vinyl chloride is 50.5% at the end of the micro- reaction of second level, and reaction mixture goes successively to three-level microreactor
203 are reacted；By terminator (N, N- diethyl hydroxylamine and tert-butyl hydroxy when the micro- reaction conversion rate of vinyl chloride of three-level is 82%
Methyl phenyl ethers anisole) be added three-level microreactor 203 obtain PVC slurry.Reaction mass is total by microreactor microchannels at different levels
Time is 18s.
(2) enter slurry tank 4 from the PVC slurry that three-level microreactor 203 comes out, vinyl chloride gas enters in slurry tank 4
Recovery system, PVC slurry are then sent into stripping system by mashing pump and remove remaining vinyl chloride, are re-fed into drying system and remove water
Point, obtain finished product Corvic.Through examining Corvic particle diameter distribution width 1.38, molecular weight distributing index exists
1.75, quality index meets GB/T5761.
Embodiment three:
The production of polyvinyl chloride is used for using above-mentioned apparatus according to the following steps:
Wherein the microchannel length of level-one microreactor described in above-mentioned apparatus 201 is 5m, and cross-sectional area is
0.5mm2；The microchannel length of the second level microreactor 202 is 10m, cross-sectional area 0.8mm2；The three-level is micro- anti-
The microchannel length for answering device 203 is 20m, cross-sectional area 0.8mm2。
(1) according to the flow proportional set, by vinyl chloride monomer, deionized water, dispersing agent, (main dispersant selects hydroxypropyl
The polyethylene that the mixture and alcoholysis degree of base cellulose and hydroxyethyl cellulose are 68% polyvinyl alcohol and alcoholysis degree is 82%
The mixture of alcohol, dispersion aids select alcoholysis degree 45% polyvinyl alcohol), initiator (diisobutyryl peroxide and peroxidating two
Carbonic acid two (3- methoxybutyl)), pH adjusting agent (ammonium hydrogen carbonate) reaction of level-one microreactor 201 is each led into as fluid
Microchannel, raw material are mixed after entering microchannel, and polymerization reaction carries out in microchannel, come from heat-exchange system 5
The reactant that enters in air-tight chamber 2001 and microchannel of circulating hot water carry out indirect heat exchange, control reaction temperature is
35 DEG C, reaction pressure 0.8Mpa；Conversion rate of vinyl chloride is 13.6% at the end of the micro- reaction of level-one, and reaction mixture is gone successively to
Second level microreactor 202 is reacted；At the end of the micro- reaction of second level conversion rate of vinyl chloride be 54.1%, reaction mixture continue into
Enter three-level microreactor 203 to be reacted；By terminator (N, N- diethyl hydroxyl when the micro- reaction conversion rate of vinyl chloride of three-level is 86%
Amine and tert-butyl hydroxy anisole) be added three-level microreactor 203 obtain PVC slurry.Reaction mass passes through microreactors at different levels
The total time of microchannel is 500s.
(2) enter slurry tank 4 from the PVC slurry that three-level microreactor 203 comes out, vinyl chloride gas enters in slurry tank 4
Recovery system, PVC slurry are then sent into stripping system by mashing pump and remove remaining vinyl chloride, are re-fed into drying system and remove water
Point, obtain finished product Corvic.Through examining Corvic particle diameter distribution width 1.35, molecular weight distributing index exists
1.65, quality index meets GB/T5761.
Example IV:
The production of polyvinyl chloride is used for using above-mentioned apparatus according to the following steps:
Wherein the microchannel length of level-one microreactor described in above-mentioned apparatus 201 is 2m, and cross-sectional area is
0.2mm2；The microchannel length of the second level microreactor 202 is 6m, cross-sectional area 0.5mm2；The micro- reaction of three-level
The microchannel length of device 203 is 13m, cross-sectional area 0.5mm2。
(1) according to the flow proportional set, by vinyl chloride monomer, deionized water, dispersing agent, (main dispersant selects hydroxypropyl
The mixture and alcoholysis degree of base cellulose and methylhydroxypropylcellulose be 68% polyvinyl alcohol and alcoholysis degree be 82% it is poly-
The mixture of vinyl alcohol, dispersion aids select alcoholysis degree 45% polyvinyl alcohol), initiator (diisobutyryl peroxide and peroxide
Change two carbonic acid two (3- methoxybutyl)), pH adjusting agent (ammonium hydrogen carbonate) as fluid each lead into level-one microreactor 201
Microchannel, raw material are mixed after entering microchannel, and polymerization reaction carries out in microchannel, from heat exchange system
The reactant that the circulating hot water of system 5 enters in air-tight chamber 2001 and microchannel carries out indirect heat exchange, control reaction temperature
Degree is 57 DEG C, reaction pressure 0.8Mpa；Conversion rate of vinyl chloride is 16.3% at the end of the micro- reaction of level-one, and reaction mixture continues
It is reacted into second level microreactor 202；At the end of the micro- reaction of second level conversion rate of vinyl chloride be 46.4%, reaction mixture after
The continuous three-level microreactor 203 that enters is reacted；By terminator (N, N- diethyl when the micro- reaction conversion rate of vinyl chloride of three-level is 85%
Base azanol) be added three-level microreactor 203 obtain PVC slurry.Reaction mass is total by microreactor microchannels at different levels
Time is 120s.
(2) enter slurry tank 4 from the PVC slurry that three-level microreactor 203 comes out, vinyl chloride gas enters in slurry tank 4
Recovery system, PVC slurry are then sent into stripping system by mashing pump and remove remaining vinyl chloride, are re-fed into drying system and remove water
Point, obtain finished product Corvic.Through examining Corvic particle diameter distribution width 1.28, molecular weight distributing index exists
1.65, quality index meets GB/T5761.
Embodiment five:
The production of polyvinyl chloride is used for using above-mentioned apparatus according to the following steps:
Wherein the microchannel length of level-one microreactor described in above-mentioned apparatus 201 is 2m, and cross-sectional area is
0.2mm2；The microchannel length of the second level microreactor 202 is 6m, cross-sectional area 0.5mm2；The micro- reaction of three-level
The microchannel length of device 203 is 13m, cross-sectional area 0.5mm2。
(1) according to the flow proportional set, by vinyl chloride monomer, deionized water, dispersing agent, (main dispersant selects hydroxypropyl
The mixture and alcoholysis degree of base cellulose and methylhydroxypropylcellulose be 68% polyvinyl alcohol and alcoholysis degree be 82% it is poly-
The mixture of vinyl alcohol, dispersion aids select alcoholysis degree 45% polyvinyl alcohol), initiator (diisobutyryl peroxide, peroxidating
Two carbonic acid two (3- methoxybutyl) are compound), pH adjusting agent (sodium hydroxide) each lead into level-one microreactor 201 as fluid
Microchannel, raw material is mixed after entering microchannel, and polymerization reaction carries out in microchannel, from heat exchange
The reactant that the circulating hot water of system 5 enters in air-tight chamber 2001 and microchannel carries out indirect heat exchange, control reaction
Temperature is 57 DEG C, reaction pressure 0.8Mpa；At the end of the micro- reaction of level-one conversion rate of vinyl chloride be 17.3%, reaction mixture after
The continuous second level microreactor 202 that enters is reacted；Conversion rate of vinyl chloride is 48.4% at the end of the micro- reaction of second level, reaction mixture
Three-level microreactor 203 is gone successively to be reacted；By terminator (N, N- bis- when the micro- reaction conversion rate of vinyl chloride of three-level is 85%
Ethylhydroxyl amine and tert-butyl hydroxy anisole) be added three-level microreactor 203 obtain PVC slurry.Reaction mass passes through at different levels micro-
The total time of reactor reaction microchannel is 120s.
(2) enter slurry tank 4 from the PVC slurry that three-level microreactor 203 comes out, vinyl chloride gas enters in slurry tank 4
Recovery system, PVC slurry are then sent into stripping system by mashing pump and remove remaining vinyl chloride, are re-fed into drying system and remove water
Point, obtain finished product Corvic.Through examining Corvic particle diameter distribution width 1.30, molecular weight distributing index exists
1.68, quality index meets GB/T5761.
Embodiment six:
The production of polyvinyl chloride is used for using above-mentioned apparatus according to the following steps:
Wherein the microchannel length of level-one microreactor described in above-mentioned apparatus 201 is 2m, and cross-sectional area is
0.2mm2；The microchannel length of the second level microreactor 202 is 6m, cross-sectional area 0.5mm2；The micro- reaction of three-level
The microchannel length of device 203 is 13m, cross-sectional area 0.5mm2。
(1) according to the flow proportional set, by vinyl chloride monomer, deionized water, dispersing agent, (main dispersant selects hydroxypropyl
The mixture and alcoholysis degree of base cellulose and methylhydroxypropylcellulose be 68% polyvinyl alcohol and alcoholysis degree be 82% it is poly-
The mixture of vinyl alcohol, dispersion aids select alcoholysis degree 45% polyvinyl alcohol), initiator (diisobutyryl peroxide, peroxidating
Neodecanoic acid tert-pentyl ester is compound), pH adjusting agent (sodium hydroxide) reaction that each leads into level-one microreactor 201 as fluid it is micro- logical
Road, raw material are mixed after entering microchannel, and polymerization reaction carries out in microchannel, from following for heat-exchange system 5
The reactant that ring hot water enters in air-tight chamber 2001 and microchannel carries out indirect heat exchange, and control reaction temperature is 57
DEG C, reaction pressure 0.8Mpa；Conversion rate of vinyl chloride is 15.5% at the end of the micro- reaction of level-one, and reaction mixture goes successively to two
Grade microreactor 202 is reacted；Conversion rate of vinyl chloride is 50.8% at the end of the micro- reaction of second level, and reaction mixture is gone successively to
Three-level microreactor 203 is reacted；By terminator (tert-butyl hydroxy benzene first when the micro- reaction conversion rate of vinyl chloride of three-level is 85%
Ether) be added three-level microreactor 203 obtain PVC slurry.The total time that reaction mass passes through microreactor microchannels at different levels
For 120s.
(2) enter slurry tank 4 from the PVC slurry that three-level microreactor 203 comes out, vinyl chloride gas enters in slurry tank 4
Recovery system, PVC slurry are then sent into stripping system by mashing pump and remove remaining vinyl chloride, are re-fed into drying system and remove water
Point, obtain finished product Corvic.Through examining Corvic particle diameter distribution width 1.32, molecular weight distributing index exists
1.63, quality index meets GB/T5761.
The above, only the utility model enumerate preferable example, do not make in any form to the utility model
With substantial limitation, it is noted that for those skilled in the art, in the premise for not departing from the utility model method
Under, the numerous improvement that can also be made and supplement, these are improved and supplement should also be as being considered as the protection scope of the utility model.It is all
In the case where not departing from the spirit and scope of the utility model, made when using the revealed content of the above utility model
Variation, modification and differentiation equivalent variations, be the equivalent embodiment of the utility model；Meanwhile it is all according to the utility model
Variation, modification and differentiation of the substantial technological to any equivalent variations made by above-described embodiment, should belong to the utility model
Technical solution in the range of.
Claims (5)
1. the continuous synthesis system of suspension type polyvinyl-chloride, it is characterised in that: including micro- reaction system (2), micro- reaction system
(2) include at least thtee-stage shiplock microreactor, the cross-sectional area of the microchannel of the microreactor is 0.1~1mm, edge
The cross-sectional area that material flow direction is connected on the microchannel of the microreactor of front end is less than series connection behind other
The cross-sectional area of the microchannel of microreactor, polymerization reaction carry out in microreactor.
2. the continuous synthesis system of suspension type polyvinyl-chloride according to claim 1, it is characterised in that: the suspension method polychlorostyrene
The continuous synthesis system of ethylene includes sequentially connected feed system (1), micro- reaction system (2) and slurry tank (3)；It further include terminating
Agent basin (4) and heat-exchange system (5), the heat-exchange system (5) connect with microreactors at different levels, the terminator basin (4) with
The connection of final stage microreactor.
3. the continuous synthesis system of suspension type polyvinyl-chloride according to claim 2, it is characterised in that: the microreactor packet
The reaction zone (2002) for including air-tight chamber (2001) and being arranged in air-tight chamber (2001), the reaction zone (2002)
It is provided at least one microchannel.
4. the continuous synthesis system of suspension type polyvinyl-chloride according to claim 3, it is characterised in that: the heat-exchange system
It (5) include the heat transferring medium inlet tube (501) being connected to the air-tight chamber of each microreactor (2001) and heat transferring medium outlet
It manages (502).
5. the continuous synthesis system of suspension type polyvinyl-chloride described in any claim, feature exist according to claim 1~4
In: micro- reaction system (2) by sequentially connected level-one microreactor (201), second level microreactor (202), three-level is micro- anti-
Device (203) are answered to form；The microchannel length of the level-one microreactor (201) be 1~5m, cross-sectional area be 0.1~
0.5mm2；The microchannel length of the second level microreactor (202) is 4~10m, and cross-sectional area is 0.3~0.8mm2；Institute
The microchannel length for stating three-level microreactor (203) is 10~20m, and cross-sectional area is 0.3~0.8mm2；And the second level
The cross-sectional area of the microchannel of microreactor (202) and three-level microreactor (203) is greater than level-one microreactor (201)
The cross-sectional area of microchannel.
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| CN (1) | CN209501640U (en) |
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2018
- 2018-11-23 CN CN201821952627.7U patent/CN209501640U/en active Active
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