CN105859928A - Optimal control method for polyvinyl chloride polymeric kettle - Google Patents
Optimal control method for polyvinyl chloride polymeric kettle Download PDFInfo
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- CN105859928A CN105859928A CN201610289524.6A CN201610289524A CN105859928A CN 105859928 A CN105859928 A CN 105859928A CN 201610289524 A CN201610289524 A CN 201610289524A CN 105859928 A CN105859928 A CN 105859928A
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- polymeric kettle
- pipe
- control method
- dispersing agent
- optimal control
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F114/00—Homopolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen
- C08F114/02—Monomers containing chlorine
- C08F114/04—Monomers containing two carbon atoms
- C08F114/06—Vinyl chloride
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2/00—Processes of polymerisation
- C08F2/01—Processes of polymerisation characterised by special features of the polymerisation apparatus used
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2/00—Processes of polymerisation
- C08F2/12—Polymerisation in non-solvents
- C08F2/16—Aqueous medium
- C08F2/20—Aqueous medium with the aid of macromolecular dispersing agents
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- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Polymerisation Methods In General (AREA)
Abstract
The invention belongs to the field of organic chemistry and provides an optimal control method for a polyvinyl chloride polymeric kettle. The method comprises optimal control of the following steps of 1, detecting before feeding, 2, filling of a secondary dispersing agent, 3, adding of an initiating agent and 4, linking of a terminating agent procedure. According to the control method for increasing the utilization rate of the polymeric kettle and improving the quality of finished resin products, when water and monomers are added, the dispersing agent filling procedure is started, the time for dispersing agent filling is shortened in the time period for water and monomer adding, on the premise of meeting process formula production, the feeding procedure is optimized, and the feeding time is shortened by about 6 min for each kettle.
Description
Technical field
The invention belongs to organic chemistry filed, be specifically related to a kind of polymer containing chlorine element
Production control method.
Background technology
Polrvinyl chloride is important industrial chemicals, has demand widely at each industrial circle.Poly-
The production method of vinyl chloride mainly includes that suspension polymerisation, polymerisation in bulk, suspension polymerisation, solution gather
Close four kinds.Emulsion suspension polymerization is the widest method that manufacturing enterprise of China uses.
It is to add deionized water and suspending agent in polymeric kettle that suspension polymerization produces, and adds and causes
Polymeric kettle is sealed after agent, air and be dissolved in the oxygen of material in vacuum removal still, it is subsequently adding chloroethene
Alkene monomer starts to warm up stirring.By stirring action, monomer dispersion becomes droplet, polyreaction
Occur in each monomer liquid pearl.Extract unreacted monomer after being polymerized out and slurry carries out vapour
Carry, reclaim Vinyl Chloride Monomer, the slurry after gas bleeding through centrifugation, be dried, sieve
After i.e. obtain product.For suspension polymerisation production technology, the control system of the many employings of manufacturing enterprise is
Distributed Control System (DCS), this control system uses intermittent batch to control, with polymeric kettle
Temperature is control core parameter, including the active station as system Yu the man-machine interface of operator.
For there being the production line of multiple polymeric kettle, in operation, operator is to exception for existing program
Situation judges to find the most easily to occur production accident, impact safety in production, the most 1. program
When adding initiator, not being adjusted polymeric kettle temperature, once initiator unit breaks down
Time, operator processes not in time, it is easy to makes still temperature, still press and rises, causes the great of implode
Accident；2., at the end of polymeric kettle reaction, program does not does terminator linkage, and needs master control to select
Adding after still operation, it is easy to maloperation, it is to avoid artificial maloperation, causing the accident.
In existing Production of PVC technique, remain in the relatively low defect of productivity ratio, but produce
Business Economic Benefit improves and must realize on the premise of safety in production.To control system optimization
Reform, improves the utilization rate of polymeric kettle in existing production system, increases polymerization production capacity, eliminates raw
Potential safety hazard present in product, is to improve production safety and automaticity, reduction PVC production
The effective way of cost.
Summary of the invention
For the weak point of art technology, the present invention controls program to polymeric kettle and has done useful
Improve.Specifically, the purpose of the present invention is to propose to the optimization control of a kind of pvc polymerizer
Method processed.
For realizing above-mentioned purpose technical scheme of the present invention it is:
The optimal control method of a kind of pvc polymerizer, controls polymeric kettle by control system
Produce, the optimal control comprised the following steps:
1) detection before pan feeding: before linkage pan feeding, detection still chuck and interior cold apron flow,
2) the filling of twice dispersing agent: while polymeric kettle adds monomer and water, carry out two
The weighing and filling of secondary dispersant；
3) initiator adds: at initiator charging process to polymeric kettle temperature detection, if polymerization
Still temperature does not meets index request, control system pop instruction, and operator confirm to participate in tandem
Regulation；Meet temperature and then add initiator；
4) terminator operation linkage: the polymeric kettle that polyreaction terminates reaches pressure drop, controls
This polymeric kettle of the interface display of system, confirms the operation that terminator adds.
Step 1) in, if undesirable, on-call maintenance circulation water regulating valve, it is to avoid reaction
Period polymeric kettle temperature control；Step 4) control to select still to operate, reduce maloperation probability.
Suspension emulsion polymerization polrvinyl chloride is carried out in described pvc polymerizer
Reaction；The monomer of polymerization is polrvinyl chloride.
Wherein, the first pipeline that described polymeric kettle top is arranged connects and has painting wall agent pipe, high pressure
Wash tub pipe and top steam pipe；Connect on the second pipeline that still top is arranged have into monomer pipe and
Still recovery tube；Connecting on the 3rd pipeline arranged bottom polymeric kettle has into dispersant pipe, enters
Twice dispersing agent pipe and enter initiator pipe, the 4th pipeline arranged bottom polymeric kettle connects have slow
Electuary pipe, enter DI, bottom steam pipe and storing pipe.
Preferably, twice dispersing is filled after being spaced 85～95s after polymeric kettle adds monomer and water
Agent；Fill twice dispersing agent afterflush pipeline, then fill a dispersant；Described once
Dispersant is polyvinyl alcohol and/or cellulose, and twice dispersing agent is polyvinyl alcohol and/or cellulose.
Described cellulose is hydroxypropyl methyl cellulose (HPMC), hydroxyethyl cellulose, carboxymethyl
One in cellulose.
Wherein, polymeric kettle temperature controls is 56～58 DEG C.Described initiator is peroxy dicarbonate
Double ethylhexyls (EHP) and/or peroxidating pungent certain herbaceous plants with big flowers acid isopropyl phenyl ester (CNP).
Wherein, when polymeric kettle pressure is down to 0.05MPa, show that polyreaction terminates, add eventually
Only agent, described terminator is organic amine terminator.
Optimal control method of the present invention, uses Distributed Control System, a collecting and distributing control
System controls 1～3 set production lines, and every production line arranges 7 polymeric kettles.
After polymeric kettle controls program optimization, one polymerization of each increase can be produced at existing two
Still, adds polyplant resin yield.Newly-increased two polymeric kettles then increase a control station.
The beneficial effects of the present invention is:
What the present invention provided improves polymeric kettle utilization rate and promotes the controlling party of resin end product quality
Method, polymeric kettle adds water with monomer when, starts dispersant to-fill procedure, is filled out by dispersant
The Time Compression filled, within the time period with monomer that adds water, is meeting the premise that technical recipe produces
Under, by pan feeding program optimization, still shortens pan feeding time about 6min；
Improvement to system control mode, with temperature when adding initiator as Con trolling index, increases
Terminator links, and needs master control adding after carrying out selecting still operation, it is easy to maloperation, it is to avoid
Artificial maloperation, causes the accident, and can effectively solve the problems referred to above after transformation；Simultaneously because
The problems referred to above have been resolved, and the polymerization pan feeding time of shortening, solve the potential safety hazard having been found that,
Based on this, polyplant has expanded 2 polymeric kettles, improves production capacity, reduces production
Cost.
Accompanying drawing explanation
Fig. 1 is the structural representation of polymeric kettle.
In figure, 1, Tu Biguan；2, buffer agent pipe；3, DI is entered；4, monomer pipe is entered；
5, twice dispersing agent pipe is entered；6, a dispersant pipe is entered；7, initiator pipe is entered；8, polymerization
Still；9, terminator pipe is entered；10, storing pipe；11, jacket of polymerization recirculated water upper hose；
12, jacket of polymerization recirculated water return pipe, 13, high pressure rinse water pipe, 14, still recovery tube；
15, bottom steam pipe；16 top steam pipes.
Detailed description of the invention
Below by most preferred embodiment, the present invention is described.Those skilled in the art should know
It is that embodiment is only used for illustrating rather than for limiting the scope of the present invention.
In embodiment, if no special instructions, means used are the means that this area is conventional.
Embodiment 1:
Polymeric kettle structure is shown in Fig. 1, the first pipeline that polymeric kettle top is arranged connects and has painting wall agent
Pipe 1, high pressure rinse water pipe 13 and top steam pipe 16；On the second pipeline that still top is arranged
Connection has into monomer pipe 4, enters terminator pipe 9 and still recovery tube 14；Arrange bottom polymeric kettle
Connecting on 3rd pipeline has into dispersant pipe 6, enters twice dispersing agent pipe 5 and enter initiator
Pipe 7, bottom polymeric kettle arrange the 4th pipeline on connect have buffer agent pipe 2, enter DI 3,
Bottom steam pipe 15 and storing pipe 10.
This enterprise has two production lines, every original 6 70m of line3Polymeric kettle, controls system
System uses Japan's Yokogawa CS3000 control system, 5 active stations of 1 engineering station (EWS)
(including an active station of drying control) (HIS), 4 set control stations (FCS includes two
The control station that newly-increased polymeric kettle increases), active station is the man-machine interface of system and operator.
Every still feed time about 50min of original control programme-control.After Optimal Control System, every
Production line arranges 7 polymeric kettles, and control system controls the production technology of polymeric kettle and is:
Detection before pan feeding: before linkage pan feeding, detection still chuck and interior cold apron flow, if inspection
Measure flow, internal hemorrhage due to trauma has been described, then on-call maintenance circulation water regulating valve, it is to avoid be poly-during reaction
Close still temperature control；
Step S1, starts polymeric kettle and is coated with still wall operation sequence, uses Italy's Huang to be coated with wall agent and is coated with
With polymeric kettle still top flushing water, polymeric kettle still wall is rinsed after wall, rushes still water from polymeric kettle still
The end, is to wastewater trough；
Step S2, starts pan feeding program and adds buffer agent ammonium hydrogen carbonate in described polymeric kettle still；
Step S3, starts into monomer and water pan feeding program, controls pan feeding water temperature and confirms to add
Amount, confirm monomer addition, simultaneously procedure auto-control weigh hopper fill twice dispersing agent gather
Vinyl alcohol；While polymeric kettle adds monomer and water, carry out weighing and filling of twice dispersing agent
Dress, shortens the pan feeding time；
Step S4, treats monomer and water mixing 90s；
Step S5, carries out the addition operation of twice dispersing agent, twice dispersing agent is added with pump
In polymeric kettle；
Step S6, opens a dispersant and adds program, with pump by a polyethylene of dispersing agent
Alcohol and hydroxypropyl methyl cellulose (HPMC), the two mass ratio is 5:1, adds polymeric kettle
In；
Step S7, waits 300s, makes step S2 to step S6 enter the raw material of still and auxiliary agent exists
The dispersion being suitable for polyreaction is formed in still；
Step S8, at initiator charging process to polymeric kettle temperature detection, if polymeric kettle temperature
Not meeting index request (temperature index requires ＞ 56 DEG C), instruction is ejected at the operation interface of system,
Operator confirm to participate in bunch grade adjustment；Jacket of polymerization recirculated water upper hose 11 and polymeric kettle
Chuck recirculated water return pipe 12 connects the whole circulation of production line, regulation polymeric kettle
Temperature；Meet the requirements, carry out initiator and add program；Observe the power curve index of polymeric kettle,
Add initiator；Initiator is the double ethylhexyl (EHP) of peroxy dicarbonate and peroxidating
Pungent certain herbaceous plants with big flowers acid isopropyl phenyl ester (CNP), mass ratio is 1:5.
Step S9, in the polymerization, main observation still temperature, still pressure, power etc. control to refer to
Mark, reaction heat polyreaction produced by chuck, interior cold apron recirculated water is removed, and protects
The safety of card polyreaction；
Step S10, when polyreaction pressure drop reaches 0.05MPa, system judges reaction knot automatically
Bundle, operation system interface ejects the icon of this polymeric kettle, and operator confirm to carry out to this still
Add the operation of terminator (organic amine terminator, purchased from Ningxia Sheng Jia Chemical Co., Ltd.),
Still need not be selected to operate, reduce maloperation probability.Terminate the polyreaction of this still；
Step S11, after terminator adds, selects discharging.
Use the control method of the present embodiment, every still pan feeding saving of time 6min, product quality
Stable, production efficiency is greatly improved；In adding terminator step, it not as original
Program occurs the icon of multiple still like that, needs operator to select, but only pressure drop reaches
The polymeric kettle of 0.05MPa occurs on operation interface, it is to avoid maloperation, improves production peace
Entirely.
Embodiment 2:
Step S1, starts polymeric kettle and is coated with still wall operation sequence, uses Italy's Huang to be coated with wall agent and is coated with
With polymeric kettle still top flushing water, polymeric kettle still wall is rinsed after wall, rushes still water from polymeric kettle still
The end, is to wastewater trough；
Step S2, starts pan feeding program and adds buffer agent ammonium hydrogen carbonate in described polymeric kettle still；
Step S3, starts into monomer and water pan feeding program, controls pan feeding water temperature and confirms to add
Amount, confirm monomer addition, simultaneously procedure auto-control weigh hopper fill twice dispersing agent gather
Vinyl alcohol；While polymeric kettle adds monomer and water, carry out weighing and filling of twice dispersing agent
Dress, shortens the pan feeding time；
Step S4, treats monomer and water mixing 90s；
Step S5, carries out the addition operation of twice dispersing agent, twice dispersing agent is added with pump
In polymeric kettle；
Step S6, opens a dispersant and adds program, with pump by a polyethylene of dispersing agent
Alcohol and hydroxyethyl cellulose (HPMC), the two mass ratio is 8:1, adds in polymeric kettle；
Step S7, waits 300s, makes step S2 to step S6 enter the raw material of still and auxiliary agent exists
The dispersion being suitable for polyreaction is formed in still；
Step S8, at initiator charging process to polymeric kettle temperature detection, if polymeric kettle temperature
Not meeting index request (temperature index requires ＞ 57 DEG C), instruction is ejected at the operation interface of system,
Operator confirm to participate in bunch grade adjustment；Meet the requirements, carry out initiator and add program；Observe
The power curve index of polymeric kettle, adds initiator；Initiator is the double diethyl of peroxy dicarbonate
The own ester of base (EHP) and peroxidating pungent certain herbaceous plants with big flowers acid isopropyl phenyl ester (CNP), mass ratio is 1:6.
Step S9, in the polymerization, main observation still temperature, still pressure, power etc. control to refer to
Mark, reaction heat polyreaction produced by chuck, interior cold apron recirculated water is removed, and protects
The safety of card polyreaction；
Step S10, when polyreaction pressure drop reaches 0.05MPa, system judges reaction knot automatically
Bundle, operation system interface ejects the icon of this polymeric kettle, and operator confirm to carry out to this still
Add the operation of terminator (organic amine terminator, purchased from Ningxia Sheng Jia Chemical Co., Ltd.),
Still need not be selected to operate, reduce maloperation probability.Terminate the polyreaction of this still；
Step S11, after terminator adds, selects discharging.
The setting of system and other operations are with embodiment 1.
Above embodiment is only to be described the preferred embodiment of the present invention, the most right
The scope of the present invention is defined, on the premise of designing spirit without departing from the present invention, and this area
Various modification that technical scheme is made by ordinary skill technical staff and improvement, all should
Fall in the protection domain that claims of the present invention determines.
Claims (7)
1. an optimal control method for pvc polymerizer, uses control system to control the production of polymeric kettle, it is characterised in that the optimal control comprised the following steps:
1) detection before pan feeding: before linkage pan feeding, detection still chuck and interior cold apron flow,
2) the filling of twice dispersing agent: while polymeric kettle adds monomer and water, carry out weighing and filling of twice dispersing agent；
3) initiator adds: at initiator charging process to polymeric kettle temperature detection, if polymeric kettle temperature does not meets index request, control system pop instruction, and operator confirm to participate in bunch grade adjustment；Meet temperature and then add initiator；
4) terminator operation linkage: the polymeric kettle that polyreaction terminates reaches pressure drop, this polymeric kettle of the interface display of control system, confirms the operation that terminator adds.
Optimal control method the most according to claim 1, it is characterised in that carry out the reaction of suspension emulsion polymerization polrvinyl chloride in described pvc polymerizer；The monomer of polymerization is vinyl chloride.
Optimal control method the most according to claim 1, it is characterised in that connect on the first pipeline that described polymeric kettle top is arranged and have painting wall agent pipe, high pressure rinse water pipe and top steam pipe；Connect on the second pipeline that still top is arranged and have into monomer pipe and still recovery tube；Connecting on the 3rd pipeline arranged bottom polymeric kettle has into dispersant pipe, enters twice dispersing agent pipe and enter initiator pipe, and the 4th pipeline arranged bottom polymeric kettle connects to be had buffer agent pipe, enter DI, bottom steam pipe and storing pipe.
4. according to the arbitrary described optimal control method of claims 1 to 3, it is characterised in that polymeric kettle fills twice dispersing agent after being spaced 85～95s after adding monomer and water；Fill twice dispersing agent afterflush pipeline, then fill a dispersant；A described dispersant is polyvinyl alcohol and/or cellulose, and twice dispersing agent is polyvinyl alcohol and/or cellulose；Described cellulose is the one in hydroxypropyl methyl cellulose, hydroxyethyl cellulose, carboxymethyl cellulose.
5. according to the arbitrary described optimal control method of claims 1 to 3, it is characterised in that it is 56～58 DEG C that polymeric kettle temperature controls；Described initiator is from the double ethylhexyl of peroxy dicarbonate and/or peroxidating pungent certain herbaceous plants with big flowers acid isopropyl phenyl ester.
6. according to the arbitrary described optimal control method of claims 1 to 3, it is characterised in that when polymeric kettle pressure is down to 0.05MPa, showing that polyreaction terminates, add terminator, described terminator is organic amine terminator.
7., according to the arbitrary described optimal control method of claims 1 to 3, it is characterised in that use Distributed Control System to control polymeric kettle and produce, a Distributed Control System controls 1～3 set production lines, and every production line arranges 7 polymeric kettles.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107621835A (en) * | 2017-08-26 | 2018-01-23 | 石河子开发区天业化工有限责任公司 | The control method of Settling tanks pressure in a kind of polymerization |
| CN110917999A (en) * | 2019-12-10 | 2020-03-27 | 昊华宇航化工有限责任公司 | Polymerization feeding optimization system and method |
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| CN102863570A (en) * | 2012-10-11 | 2013-01-09 | 江苏省格林艾普化工股份有限公司 | Seventy cubic meter polymeric kettle feeding process for producing polrvinyl chloride |
| CN104028173A (en) * | 2014-05-28 | 2014-09-10 | 新疆中泰化学股份有限公司 | Polymerizer feeding device and using method thereof |
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| CN102863570A (en) * | 2012-10-11 | 2013-01-09 | 江苏省格林艾普化工股份有限公司 | Seventy cubic meter polymeric kettle feeding process for producing polrvinyl chloride |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107621835A (en) * | 2017-08-26 | 2018-01-23 | 石河子开发区天业化工有限责任公司 | The control method of Settling tanks pressure in a kind of polymerization |
| CN107621835B (en) * | 2017-08-26 | 2020-01-07 | 石河子天域新实化工有限公司 | Method for controlling pressure of settling tank in polymerization production |
| CN110917999A (en) * | 2019-12-10 | 2020-03-27 | 昊华宇航化工有限责任公司 | Polymerization feeding optimization system and method |
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