CN205420252U - A apparatus for producing for polyvinyl chloride seed law paste resin - Google Patents
A apparatus for producing for polyvinyl chloride seed law paste resin Download PDFInfo
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- CN205420252U CN205420252U CN201620277564.4U CN201620277564U CN205420252U CN 205420252 U CN205420252 U CN 205420252U CN 201620277564 U CN201620277564 U CN 201620277564U CN 205420252 U CN205420252 U CN 205420252U
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Abstract
The utility model relates to a PVC paste paste resin's field, especially an apparatus for producing for polyvinyl chloride seed law paste resin. Preparation jar is connected with the top of polymerization cauldron and seed polymerization cauldron through the pipeline respectively, and the bottom of seed reation kettle and polymerization cauldron is connected with the wastewater collection groove respectively, seed reation kettle passes through the seed storage tank and gets together the reation kettle top to be connected, the wastewater collection groove is passed through the strip tower and is connected with the polymerization cauldron and constitutes circulation circuit, and polymerization cauldron bottom is connected with blowpit and desorption tower, and the export pipeline of blowpit is connected with defoaming mechanism, and the pipeline of defoaming mechanism and strip tower converges the back and is connected with the gas holder, the desorption tower is connected with the drying tower, and the drying tower passes through the bag hose and is connected with the finished product bin. Through the production technology that the device goes on, compare with prior art, need not to add chemical defoaming agent among the recovery process, sewage reaches the serialization to be handled, increases substantially loading and unloading capacity, reduces intensity of labour, reduction in production cost.
Description
Technical field
The present invention relates to the field of a kind of polrvinyl chloride mush resin, a kind of process units sticking with paste resin for the polrvinyl chloride seed law.
Background technology
Polrvinyl chloride (PVC) sticks with paste resin as the term suggests being that this kind of resin is mainly applied making paste forms, and people commonly use this kind and stick with paste and be referred to as plasticized paste, is a kind of unique liquid form of igelite under rough.Sticking with paste resin often to be prepared by emulsion and microsuspending method, its reaction equation is:
nCH2=CHCL → (CH2-CHCL) n.
PVC paste resin is fine because of granularity, and its quality, as Pulvis Talci, has nonflowing character.PVC paste resin is agitated to form stable suspension after mixing with plasticizer, i.e. makes PVC paste material, or referred to as PVC plasticized paste, PVC colloidal sol, and people are used for being processed into end article the most in this form.During paste producing, according to different goods needs, add various filler, diluent, heat stabilizer, foaming agent and light stabilizer etc..
The development of PVC paste Resin Industry, it is provided that the most heated a kind of novel liquid material just becoming polrvinyl chloride product.This kind of liquid material configuration is convenient; stable performance, easy to control, easy to use, product properties is excellent, chemical stability is good; there are certain mechanical strength, easy coloring etc., be therefore widely used in artificial leather, flooring laminate, medical, precision instrument produce and the production of industry (electronic handle medical apparatus and instruments, labor protection glove etc.), paint, foamed plastic, conveyer belt, automobile decoration etc. is moulded in the elastomeric glove of catering trade, vinyl toy, soft trade mark, wallpaper, leaching.
Compared with traditional suspending resin, PVC paste resin has the advantage that
(1) process equipment is inexpensive；(2) mould simple cheap；(3) can be made into F-SP；(4) foaming is easily；(5) the goods number of times that is heated is few, it is possible to a small amount of, multi items produces.
Whole world paste PVC resin industry develops with fast speed always, and the most nearly ten years, production capacity and yield are that saltatory increases, and increase the most significant in Asia.2014, polyvinyl chloride resin aggregated capacity about 5,500,000 tons/year, China's production capacity about 710,000 tons were stuck with paste in the whole world, account for whole world aggregated capacity 13%.
Preparation method mainly has
1. emulsion method emulsion polymerization formula mainly has VCM, water, water soluble starter and emulsifying agent.Stirring is required very strict by emulsion polymerization, and initiation is carried out in aqueous phase, and normally used initiator is the oxidation-reduction system of water soluble persulfates and sulphite, and response speed is relevant with the addition speed of reducing agent and amount.Generally, the serum particle diameter that emulsion polymerization obtains, less than 0.2 μm, in order to reach to increase the purpose of serum particle diameter, develops emulsion seeded polymerization, makes serum particle diameter increase to about 1.0 μm.In emulsion is polymerized, if with the presence of the high polymer serum generated, controlling material proportion and condition, VCM is only polymerized on the serum particle generated in principle, and no longer forms new particle；This high polymer serum generated just looks like crystal seed, because of referred to herein as emulsion seeding polymerization.Not only there is rational particle diameter, it is necessary to there is suitable particle diameter distribution, just can obtain the PVC paste resin of function admirable.In emulsion polymerization, emulsifying agent is critically important, and quantity used determines the population of initiator, and the size of final serum particle has been risen Main Function.Especially when carrying out seed and generating, use high trigger rate and low-concentration emulsifier to produce, serum particle size distribution can be made to narrow.
2. microsuspending method microsuspension polymerization is to prepare a kind of method that PVC paste resin is newer, and its flow process is: the method for VCM, oil-soluble initiator, emulsifying agent and water mechanical homogenization is first made stable emulsus (particle diameter is about 1.0 μm), is then polymerized.The mobility of the PVC paste resin produced in this way is excellent, and emulsifier is few, and heat stability and the water-resistance of resin are all improved.This production technology need to pay special attention to following influence factor: selects suitable compound emulsifying agent and granule modifying agent system；The homogenizing of polymerization system component；Mixing speed；Water is appropriate with the ratio of monomer.It it is most widely used method in current world wide.Also it will not go into details herein for some modification methods such as mixing method etc..
Traditional vinyl chloride seed method polymerization is divided into raw material to prepare, seed preparation and post polymerization, recovery blowing, be spray-dried, pulverize, several steps such as the semi-automatic process of sewage, there is following aspect not enough:
1) seed preparation and post polymerization: still type is less, is 24m to the maximum3。
2) blowing is reclaimed: for reclaiming in still, reclaiming blowing time about 4～5 hours, production efficiency is low；Recovery monomer can take the foam containing serum out of need to add chemistry defoamer, because adding this defoamer, can affect paste resin Downstream processing；After recovery blowing terminates, needing every still open manhole cover high-pressure wash polymeric kettle manually, cleaning quality is affected by human factors relatively big, and danger is higher, and labor intensity is big.
3) it is spray-dried and pulverizes: for negative pressure transportation, fed distance is restricted；Drying tower needs high-pressure wash manually, and cleaning quality is affected by human factors relatively big, and danger is higher, and labor intensity is big；VC content in emission is all in more than 200ppm, not met environmental requirement.
4) sewage disposal: use semi-automatic process technique, need to remove mud cake on filter cloth with artificial.
Traditional technique and equipment exist a lot of not enough, make device production cycle length (2 stills/day), production capacity low (reclaim blowing and artificial clear still takies 8-10 hour), product quality is the best, and (agitator tank is less, machinery emulsification is incomplete, need to add chemistry defoamer), labor intensity big (mud cake on manual operation cleaning equipment, artificial removing filter cloth), and key equipment polymeric kettle volume is little, cost is caused to remain high.
Summary of the invention
It is an object of the invention to provide a kind of recovery without adding process units and the production technology thereof of sticking with paste resin for the polrvinyl chloride seed law of chemistry defoamer.
The process units of the present invention adopts the following technical scheme that
A kind of process units sticking with paste resin for the polrvinyl chloride seed law, including preparation tank, storage tank, polymerization reaction kettle, Seeded polymerization still, blowpit, removing tower, drying tower, preparation tank is connected with the top of polymerization reaction kettle and Seeded polymerization still by pipeline respectively, storage tank is connected with seed reactor and polymerization reaction kettle top respectively, and the bottom of seed reactor and polymerization reaction kettle is connected with waste water collection tank respectively；Seed reactor is connected with polymerization reaction kettle top by seed storage tank；Waste water collection tank is connected and constitutes closed circuit by stripper with polymerization reaction kettle, and polymerization reaction kettle bottom is connected with blowpit and removing tower, and the export pipeline of blowpit is connected with froth breaking mechanism, and froth breaking mechanism is connected with gas holder after converging with the pipeline of stripper；Removing tower is connected with drying tower, and drying tower is connected with finished product bin by bag hose.
The preferred version of the process units used is:
Gas holder is connected with vinyl chloride MONOMER RECOVERY tank by rectifier unit, and Vinyl Chloride Monomer recycling can is connected with polymerization reaction kettle.
Preparation tank is divided into Vinyl Chloride Monomer preparation tank, hot desalinized water preparation tank and cold desalted water preparation tank；Aforementioned three preparation tanks are connected with polymerization reaction kettle respectively.
Stripper is connected with equalization basin, and equalization basin is connected with measuring tank, and measuring tank is connected with the most mixed slow mixed groove, mixes slow mixed groove soon and is connected with neutralization chamber, and neutralization chamber is connected with the floating groove that removes, and floats except groove is connected with sand filter and centrifuge respectively.
Storage tank is divided into four kinds, is emulsifying agent storage tank, catalyst storage tank, initiator storage tank and buffer agent storage tank respectively.
Blowpit passes sequentially through dynamic defoaming mechanism, static froth breaking mechanism is connected with gas holder.
Blowpit is connected with VC removing tower by wet crushing mill, serum delivery pump.
VC removing tower is connected with drying tower by latex groove.
Drying tower passes sequentially through one-level bag hose, hopper, pulverizer, two grades of bag hoses are connected with finished product bin, and finished product bin is connected with automatic packaging system.
Seed reactor and polymerization reaction kettle are stainless steel cauldron, the volume of seed reactor at 30～55 cubic metres, polymerization reaction kettle and volume at 65～90 cubic metres.
The production technology of the present invention adopts the following technical scheme that
Production technology, whole process is controlled by DCS, carries out as follows:
, prepared by raw material:
Vinyl Chloride Monomer, desalted water are respectively by delivering in respective preparation tank outside battery limit (BL), additive is stored by respective storage tank；Vinyl Chloride Monomer is sent in seed reactor and polymerization reaction kettle as part charging for the first time；
, prepared by seed:
Hot desalinized water is by being pumped into seed reactor and polymerization reaction kettle, and emulsifying agent is initially added into when reaction, and other additives pass through pump from storage tank seed injection reactor and polymerization reaction kettle；
By initial vacuum pump by polymerization reaction kettle evacuation, when in polymerization reaction kettle, pressure declines abundant, Vinyl Chloride Monomer is added to polymerization reaction kettle by preparation tank；When adding a part of fresh Vinyl Chloride Monomer, polymerization cycle starts；
Time when Seeded polymerization still pressure declines, cooling valve closedown, polymerization terminates；When Seeded polymerization still pressure is down to 0.0Mpa, emulsion seed enters seed storage tank；
, post polymerization:
Hot desalinized water delivers to polymerization reaction kettle, and additive adds polymerization reaction kettle simultaneously, subsequently, emulsion seed adds polymerization reaction kettle, and then, the fresh Vinyl Chloride Monomer of another part adds polymerization reaction kettle, starts polyreaction；Reaction pressure declines after bulk polymerization speed slows down, and polymerization terminates；
, reclaim store:
When polymerization reaction kettle pressure is down to 0.2～0.6Mpa, discharge of materials to blowpit reclaims and stores；
, blowing reclaim froth breaking；
When the pressure in blowpit is down to 0.2～0.8Mpa, starting discharging and reclaim, serum carries out defoaming treatment by Defoaming machine；
, VC reclaim removing:
Delivering in removing tower by above-mentioned serum, reclaim VC monomer further, after the VC monomer not being recovered enters gas holder, return again to recycling can, seed reactor to be again introduced into and polymerization reaction kettle carry out the course of reaction of next time；
VC monomer after recovery, enters and is dried groove；
, be spray-dried, pulverize:
Serum in dry groove delivers to spray dryer, and the resin after being dried enters bag hose and is collected, and delivers to warehouse for finished product after pulverizing；
, waste water automatically processes continuously:
From storage tank, seed reactor, polymerization reaction kettle, blowpit, drying tower discharge wastewater collection waste water collection tank, after treatment, deliver to treatment center of sewage.
The preferred version of the production technology used is:
StepIn, Vinyl Chloride Monomer, except as part charging for the first time, afterwards, is continuously added to materials when polyreaction；Desalted water is placed in cold storage tank, for room temperature desalted water；Hot tank stores 60 DEG C of desalted waters, is heated to 60 DEG C by being passed through steam, and the desalted water in cold storage tank and the hot desalinized water in hot tank are all delivered in seed reactor and polymerization reaction kettle.
StepIn, the emulsifying agent in additive is for the preparation of emulsion seed and polymerization, and emulsifying agent is a kind of and water dissolvable thing, is pre-dissolved in addition reactor in storage tank；
Catalyst once adds in seed reactor and polymerization reaction kettle with desalted water；Buffer agent is set to two kinds: phosphoric acid and Caustic soda, and phosphoric acid is mended and added in seed reactor, and Caustic soda is added in polymerization reaction kettle；
Initiator is a kind of and water dissolvable peroxide, is continuously added in polymerization reaction kettle by initiator groove.
StepIn, additive also includes anti-fouling agent and terminator, and anti-fouling agent is placed in anti-fouling agent tank, and anti-fouling agent sprays in polymerization reaction kettle；Terminator is placed in terminator tank, in the case of polymerization is out of control, injects terminator and terminates course of reaction.
StepIn, hot desalinized water is from storage tank, with being pumped into seed reactor；Emulsifying agent (EM1) is to add when reaction starts, to form polyvinyl chloride particles；Other additives pass through pump from respective preparation tank, seed injection reactor；Before adding vinyl chloride, the air in emptying seed reactor and polymerization reaction kettle；With initial vacuum pump by seed reactor and polymerization reaction kettle evacuation；As reacting kettle inner pressure 620-680mmHg, VCM adds from fresh vinyl chloride storage tank pump-metered；
Rising when loading VCM monomer, polymerization cycle starts to start；When reactor pressure declines, cools down valve closedown, after polymerization terminates, naturally reclaim, when seed reactor pressure is down to 0.0Mpa, enters seed trough by filter and store, and analyze size with standby；
Automatically clean carrying out quick, safe closed high pressure inside seed reactor afterwards, high-pressure water pressure 25～35Mpa, DCS control cleaning step；
Cleaning is rinsed with pressure automatic spray in closed after completing again, carries out feeding tube cleaning systems afterwards, carries out the airtight automatic spraying of polymeric kettle antitack agent afterwards, waits next batch reaction operation；Wherein waste water is unified is collected in waste water tank.
StepIn, when polymerization reaction kettle pressure is down to 0.2～0.6Mpa, discharge of materials to blowpit reclaims and stores；Afterwards polymerization reaction kettle inside is carried out enclosed high pressure to clean, DCS control cleaning step；Cleaning is rinsed with pressure automatic spray in airtight work after completing again, carries out feeding tube cleaning systems afterwards, carries out the airtight automatic spraying of polymerization reaction kettle antitack agent afterwards, waits next batch reaction operation, and wherein waste water unification is collected in waste water tank.
StepIn, use negative pressure reclaim, when in blowpit pressure be down to 0.2～0.8Mpa time, start vacuum pump start discharging reclaim, until pressure reaches to terminate when-400～-700mmHg in blowpit；When blowpit carries out negative pressure recovery, steam is passed directly into blowpit heat up, serum temperature is made to reach 40 DEG C～80 DEG C, carry out in blowpit in time pushing back receipts and negative pressure recovery (certainly pushing back receipts: the pressure that VCM monomer reaction itself is carried is from blowpit release of pressure), negative pressure reclaims: when in blowpit, the pressure of release of pressure is down to 0.2～0.8Mpa, start vacuum pump to force to extract out, system can take emulsifying agent and the serum that foam includes out of, defoaming treatment is carried out via dynamically rotation mechanical realization equipment and static constructions equipment, after the serum that is captured returns to blowpit, it is pumped to drying system again be dried, chemistry defoamer is added to carry out froth breaking therebetween without to note.
StepIn, serum carries out wet grinding by the Coarse Aggregate that serum is carried secretly by Shi Shi disintegrating machine, then by pump, from blowpit delivery pump, serum is delivered to VC removing tower recovery froth breaking, is pumped into serum the most again and is dried groove, to guarantee the conversion of interval and continuous process；PVC serum, through firing equipment, is sent in removing tower via the spraying of first order removing tower, and PVC serum can be distributed in Ta Bishang, it is heated to temperature and controls at 50 DEG C～80 DEG C, vacuum degree control is-400～-700mmHg, and after demulsification, the content of vinylchloride in serum is down to below 300ppm by 2000ppm；The time of staying of serum is 3～6 hours.
StepIn, the serum being dried in groove by Shi Shi pulverizer and is pumped to spray dryer, and the resin after being dried enters bag hose and is collected, more size-reduced machine carries out the broken work of numerical value, delivers to warehouse for finished product after being delivered to finished product bin with malleation；The pressure control range of malleation conveying: 3000～5000mmH2O；Slurry in spray dryer running is attached to Ta Bishang, can effectively be cleaned up by tower wall via automatic high pressure cleaning equipment.
StepIn, from storage tank, seed reactor, polymerization reaction kettle, blowpit, drying tower discharge wastewater collection waste water collection tank, in waste water, VC content is 3000～5000ppm；Waste water, after stripper strips, reclaims residual VC, VC content in waste water and is down to below 100ppm, wastewater collection is in waste water equalization basin, COD content 2000～3000ppm, SS content 3000～5000ppm, then it is floating except groove to import air Self-pressurizing agri after fast mixed slow mixed, strike off the mud of concentration, sludge pumping is to centrifuge, and dehydration is sold after collecting into mud cake packaging, floats and carries out Automatic continuous process except rear waste water delivers to sand filtration tank, COD content is down to below 200ppm, then delivers to the process of waste water processing center.
Before vinyl chloride condenses, reclaim vinyl chloride stabilizer and liquid Caustic soda injection treatment；Process together with low oxygen content vinyl chloride, it is to avoid the formation of any vinyl collection polyperoxide；Enter stabilizer by metering infusion, enter caustic soda by infusion.
Using the present invention of technique scheme compared with prior art, without adding chemistry defoamer in removal process, sewage can reach continuous treatment, increases substantially production capacity, reduces labor intensity, reduces production cost.
Accompanying drawing explanation
Fig. 1 is the process chart of the present invention.
Detailed description of the invention
Below in conjunction with the accompanying drawings and embodiment describe in detail the present invention:
nullA kind of process units sticking with paste resin for the polrvinyl chloride seed law，See accompanying drawing 1，In figure: sand filter 1、Floating except groove 2、Neutralization chamber 3、Fast mixed slow mixed groove 4、Measuring tank 5、Equalization basin 6、Stripper 7、First vacuum pump 8、First centrifuge 9、Vinyl Chloride Monomer recycling can 10、VCM monomer preparation tank 11、Hot desalinized water preparation tank 12、Cold desalted water preparation tank 13、Waste water collection tank 14、Emulsifying agent storage tank 16A、Catalyst storage tank 16B、Initiator storage tank 16C、Buffer agent storage tank 16D、Second centrifuge 17、3rd centrifuge 18、4th centrifuge 19、5th centrifuge 20、6th centrifuge 21、First seed storage tank 22、Second seed storage tank 23、Seed reactor 24、First concentrates charge pipe 25、First cleans and spraying mechanism 26 automatically、Second cleans and spraying mechanism 27 automatically、Concentrate charge pipe 28、Polymerization reaction kettle 29、Rectifier unit 30、Gas holder 31、Second vacuum pump 32、Static froth breaking mechanism 33、Dynamic defoaming mechanism 34、Blowpit 35、Thick wet crushing mill 36、Thin wet crushing mill 37、Serum delivery pump 38、First vapor removal tank 39A、First serum mixing channel 40A、First Defoaming machine 41A、Oneth VC removing tower 42A、
Second vapor removal tank 39B, the second serum mixing channel 40B, the second Defoaming machine 41B, the 2nd VC removing tower 42B, latex groove 43, serum dosing pump 44, drying tower the 45, the 3rd clean spraying mechanism 46, one section of bag hose 47, screen cloth 48, hopper 49, pulverizer 50, two-stage nitration bag hose 51, finished product bin 52, automatic packaging system 53 automatically.
VCM monomer preparation tank 11 is connected with the top of polymerization reaction kettle 29 and Seeded polymerization still 24 by pipeline respectively, emulsifying agent storage tank 16A, catalyst storage tank 16B, initiator storage tank 16C, buffer agent storage tank 16D top with seed reactor 24 and polymerization reaction kettle 29 respectively is connected, and the bottom of seed reactor 24 and polymerization reaction kettle 29 is connected with waste water collection tank 14 respectively；Seed reactor 24 is connected with polymerization reaction kettle 29 top by seed storage tank；Seed storage tank is set to two；First seed storage tank 22 and second seed storage tank 23.
Waste water collection tank 14 is connected with seed reactor 24 and polymerization reaction kettle 29 by stripper 7 and is constituted closed circuit, polymerization reaction kettle 29 bottom is connected with blowpit 35 and VC removing tower 42, the export pipeline of blowpit 35 is connected with froth breaking mechanism, froth breaking mechanism is made up of dynamic defoaming mechanism 34 and static froth breaking mechanism 33, and froth breaking mechanism is connected with gas holder 31 after converging with the pipeline of stripper 7；VC removing tower 42 is connected with drying tower 45, and drying tower 45 is connected with finished product bin 52 by bag hose.
Gas holder 31 is connected with vinyl chloride MONOMER RECOVERY tank 10 by rectifier unit 30, and Vinyl Chloride Monomer recycling can 10 top with polymerization reaction kettle 29 again is connected.
Preparation tank is made up of Vinyl Chloride Monomer preparation tank 11, hot desalinized water preparation tank 12 and cold desalted water preparation tank 13；Aforementioned three preparation tanks, each preparation tank is connected with seed reactor 24 and polymerization reaction kettle 29 respectively.
Being provided with first on seed reactor 24 automatically to clean spraying mechanism 26 and first and concentrate charge pipe 25, first concentrates charge pipe 25 to deliver to after being converged by the pipeline of storage tank, cold desalted water preparation tank 13 and hot desalinized water preparation tank 12 three in seed reactor in 24.
Being provided with second on polymerization reaction kettle 29 and automatically clean spraying mechanism 28 and the second concentration charge pipe 27, second concentrates charge pipe 27 to be put together by the material that storage tank, the first seed storage tank 22, second seed storage tank 23, VCM monomer preparation tank 11, hot desalinized water preparation tank 12, cold desalted water preparation tank 13 and Vinyl Chloride Monomer recycling can 10 carry is delivered in polymerization reaction kettle 29.
Stripper 7 is connected by pipeline with equalization basin 6, and equalization basin 6 is connected with measuring tank 5, and measuring tank 5 is connected with the most mixed slow mixed groove 4, mixes slow mixed groove 4 soon and is connected with neutralization chamber 3, and neutralization chamber 3 is connected with the floating groove 2 that removes, and floats except groove 2 is connected with sand filter 1 and the first centrifuge 9 respectively；First centrifuge 9 is sold after pug is delivered to mud part packaging.
Being formulated with a kind of additive in storage tank, additive includes emulsifying agent, catalyst, initiator and buffer agent；
Additive is placed in respective storage tank, and storage tank is divided into four kinds, is emulsifying agent storage tank, catalyst storage tank, initiator storage tank and buffer agent storage tank respectively.
Additive also includes that anti-fouling agent and terminator, every class additive are respectively placed in respective storage tank: anti-fouling agent is placed in anti-fouling agent storage tank, and anti-fouling agent sprays in polymerization reaction kettle 29 etc.；Terminator is placed in terminator tank, in the case of polymerization is out of control, injects terminator and terminates course of reaction.
Blowpit 35 passes sequentially through dynamic defoaming mechanism 34, static froth breaking mechanism 33 is connected with gas holder 31；Blowpit 35 is arranged horizontal by heeling condition, and blowpit 35 and horizontal plane exist the angle of 5 to 10 degree.
Blowpit 35 passes sequentially through thick wet crushing mill 36, thin wet crushing mill 37, serum delivery pump 38 first serum mixing channel 40A and VC removing tower 42A and connects；First serum mixing channel 40A and the first vapor removal tank 39A connects；2nd VC removing tower 42B is by latex groove 43, serum dosing pump 44 and is connected；It is provided with the 3rd on drying tower 45 automatically to clean and spraying mechanism 46.
Drying tower 45 passes sequentially through one-level bag hose 47, screen cloth 48, hopper 49,50, two grades of bag hoses 51 of pulverizer are connected with finished product bin 52, and finished product bin 52 is connected with automatic packaging system 53.
Seed reactor 24 and polymerization reaction kettle 29 are stainless steel cauldron, and both are totally-enclosed jacket structured.The volume of seed reactor 24 is at 30～55 cubic metres, and the volume of polymerization reaction kettle 29 is at 65～90 cubic metres.
Embodiment of the method 1:
The specification of the present embodiment reactor 24 of seed selection selects 35 to stand six meters, and the specification of polymerization reaction kettle 29 selects 80 cubic metres.
Apparatus of the present invention are based under security consideration, the reaction of polymerization reaction kettle uses the airtight continuation mode being not turned on manhole cover to carry out in normal service, thus improve the quality of product and production efficiency and safe operation, full production operation process is carried out as follows by DCS control, the concrete technological process of production:
One, prepared by raw material:
1), Vinyl Chloride Monomer is by out-of-bounds delivering in respective VCM monomer preparation tank 11, desalted water is by delivering in hot desalinized water preparation tank 12 outside battery limit (BL), hot desalinized water preparation tank 12 stores 60 DEG C of desalted waters, it is heated to 60 DEG C by being passed through steam, the room temperature desalted water stored in cold desalted water preparation tank 13 is pumped in seed reactor 24 and polymerization reaction kettle 29 by the 5th centrifugal pump 20, and cold desalted water is used for cleaning seed reactor 24 and polymerization reaction kettle 29.
Hot desalinized water is by the 4th centrifugal pumping to seed reactor 24 and polymerization reaction kettle 29.
Additive is prepared by respective storage tank and is stored respectively；Vinyl Chloride Monomer is sent in seed reactor 24 and polymerization reaction kettle 29 as part charging (accounting for Vinyl Chloride Monomer cumulative volume 1/3 ~ 1/6) for the first time.
2), prepared by emulsifying agent (about 200 ~ 350Kg)
Being polymerized of the different trades mark uses different surface action agent:
(the different trades mark uses different emulsifying agents for the polymerization of the preparation of emulsion seed and each trade mark for a-emulsifying agent (EM1), b-emulsifying agent (EM2), c-emulsifying agent (EM3), they are a kind of with water dissolvable thing, be emulsifying agent groove be pre-dissolved be continuously added in seed reactor 24 with in polymerization reaction kettle 29.
3), prepared by catalyst (about 1 ~ 4Kg)
Being pre-dissolved (being also and water-soluble substance) at pre-fluid bowl by the mode similar with emulsifying agent, catalyst AC1 and AC2, AC1 are disposably to add seed reactor with desalted water by desalted water pipeline；AC2 disposably adds polymerization reaction kettle by desalted water pipeline with desalted water.4), buffer agent
Two kinds of buffer agents, phosphoric acid about 14～17kg and Caustic soda 15～18kg are by with entering to add in seed reactor 24 and polymerization reaction kettle 29, to guarantee that pH value is between 7～8.
5), initiator
The polymerization of the different trades mark uses different initiators, according to the polymerization selection one of the different trades mark:
CAT1, CAT2 are a kind of and water dissolvable peroxide (both are 4～7kg respectively), be initiator groove be pre-dissolved be continuously added to seed reactor in be first prepared as seed, participate in polyreaction in adding polymerization reaction kettle with seed form the most again.For powder shape, storage form be 25 kilograms packed, storage temperature not can exceed that 27 DEG C.
6), anti-fouling agent
The anti-fouling agent of 4～12L transfers to anti-fouling agent tank from basin with 0.3～0.9Mpa；Anti-fouling agent is to spray into polymerization reaction kettle by 1.2～2.0Mpa steam jet ejectors, produces fog in polymerization reaction kettle, makes biologically active prod cover all inwalls of reactor.
7), terminator
Under polymerization out-of-control condition, inject about 12Kg terminator and terminate course of reaction；Seed reactor 24 and polymerization reaction kettle 29 are equipped with two terminator tanks, all fill terminator solution, and are in 1.6～2.5MPa nitrogen seal pressures.
Two, prepared by seed:
Hot desalinized water 30 cubic metres, (by the way of heating, desalted water can also be become hot desalinized water) is transported to seed reactor 24 and polymerization reaction kettle 29 by the 4th centrifugal pump 19, emulsifying agent is initially added into when reaction, and other additives pass through pump from storage tank seed injection reactor 24 and polymerization reaction kettle 29.
By initial vacuum pump 32 by polymerization reaction kettle 29 evacuation, when in polymerization reaction kettle 29, pressure is down to 620～680mmHg(0.062 ~ 0.068MPa) time, Vinyl Chloride Monomer is added to polymerization reaction kettle 29 by VCM monomer preparation tank 11；Before adding vinyl chloride, the air in emptying seed reactor and polymerization reaction kettle reactor, when adding the fresh Vinyl Chloride Monomer accounting for volume ratio 1/3, the cumulative volume of Vinyl Chloride Monomer is 45 cubic metres, and polymerization cycle starts.
Time when Seeded polymerization still 29 pressure declines about 0.4Mpa, cooling valve closedown, polymerization terminates；When seed reactor 24 pressure is down to 0.0Mpa, emulsion seed, in filter enters the first seed storage tank 22 and second seed storage tank 23, analyzes size with standby；Size is about between 0.3～0.55 micron.
Afterwards seed reactor 24 inside is carried out quick, safe closed high pressure and automatically clean (high-pressure water pressure 25～35Mpa), DCS control cleaning step.
Cleaning is rinsed with pressure automatic spray in closed after completing again, carries out feeding tube cleaning systems afterwards, carries out the airtight automatic spraying of polymerization reaction kettle 29 anti-adhesion agent afterwards, waits next batch reaction operation；Wherein waste water is unified is collected in waste water collection tank 10.
The temperature operating ranges of seed reactor 24: 45～55 DEG C；The cleaning way of seed reactor 24: closed high pressure cleans automatically, pressure limit: 25～35Mpa.
The spray irrigation mode of seed reactor 24: in closed, pressure is cleaned automatically, pressure limit: 2.5～4.0MPa；Seed reactor 24 anti-adhesion agent spraying method: airtight automatic spraying.
Seed reactor 24 purging system, spray irrigation and anti-adhesion agent spraying all use DCS to control.
Polymerization reaction kettle 29 chuck form: total closed type；The special whipped form of polymerization reaction kettle 29: two-layer SANYE stirs, band baffle plate.
The pressure limit during discharging of polymerization reaction kettle 29: 0.2～0.6Mpa；The cleaning way of polymerization reaction kettle 29: closed high pressure cleans automatically, pressure limit: 25～35Mpa；The spray irrigation mode of polymerization reaction kettle 29: in closed, pressure is cleaned automatically, pressure limit: 2.5～4.0MPa.The anti-adhesion agent spraying method of polymerization reaction kettle 29: airtight automatic spraying.
The cleaning of polymerization reaction kettle 29, spray irrigation and anti-adhesion agent spraying all use DCS to control.
The seed preparation of the application of the invention and post polymerization step, can improve production capacity 50%, reduces labor intensity, it is achieved 45～50 batches are not switched on kettle cover and produce continuously.
Three, post polymerization:
Hot desalinized water delivers to polymerization reaction kettle 29, and four kinds of additives are simultaneously added polymerization reaction kettle 29, subsequently, emulsion seed is added polymerization reaction kettle 29, then, another part (remove for the first time part add with outer portion) fresh Vinyl Chloride Monomer adds polymerization reaction kettle 29, starts polyreaction；Reaction pressure declines after bulk polymerization speed slows down, and polymerization terminates.
The use of initiator (CAT1 or CAT2 depends on the trade mark), is that the heat discharged by reaction controls；Controlled to add the flow velocity of initiator by the temperature of seed reactor 24 and polymerization reaction kettle 29.
Polymerization reaction kettle 29 is cooled down by total enclosing chuck, and is cooled down by condenser.
For polymerization, only part vinyl chloride is being initially added；Remaining vinyl chloride is to add in polymerization process, and the flow being continuously added to vinyl chloride is to determine according to reaction rate.
Reactor operating condition is different, such as due to the difference of production product grade: when producing the product that the degree of polymerization is 1000, reaction temperature controls at about 45～65 DEG C, and Stress control is at 5～9 kgfs.
Four, storage is reclaimed:
When polymerization reaction kettle pressure is down to 0.2～0.6Mpa, discharge of materials to blowpit 35 reclaims and stores.
Reaction pressure will decline after bulk polymerization speed slows down, and show that polymerization terminates.When polymeric kettle pressure is down to 0.2～0.6Mpa, by discharge of materials to blowpit 35(blowpit 35 slant setting, with the angle that ground exists 5～10 degree) reclaim storage.
Afterwards polymerization reaction kettle 29 inside is carried out enclosed high pressure and automatically clean (high-pressure water pressure 25～35Mpa), DCS control cleaning step.
Cleaning is rinsed with pressure automatic spray in closed after completing again, carries out feeding tube cleaning systems afterwards, carries out the airtight automatic spraying of polymerization reaction kettle 29 anti-adhesion agent afterwards, waits next batch reaction operation；Wherein waste water is unified is collected in waste water collection tank 14.
Five, blowing recovery froth breaking:
Employing negative pressure reclaims, and when the pressure in blowpit 35 is down to 0.2～0.8Mpa, starts discharging and reclaims, and serum carries out defoaming treatment by Defoaming machine；Start vacuum pump and start discharging recovery, until pressure reaches to terminate when-400～-700mmHg in blowpit 35；When blowpit 35 carries out negative pressure recovery, steam is passed directly into blowpit 35 heat up, the pressure limit 0.2～0.5Mpa of steam, serum temperature is made to reach 40 DEG C～80 DEG C, carry out in blowpit 35 in time pushing back receipts and negative pressure recovery (certainly pushing back receipts: the pressure that VCM monomer reaction itself is carried is from blowpit release of pressure), negative pressure reclaims: when in blowpit 35, the pressure of release of pressure is down to 0.2～0.8Mpa, start vacuum pump to force to extract out, system can take emulsifying agent and the serum that foam includes out of, defoaming treatment (dynamic defoaming mechanism 34 is carried out via dynamic defoaming mechanism 34 and static froth breaking mechanism 33, specification EM-431, Kunshan Yongsheng Products；Static froth breaking mechanism 33, model: EC-431), after the serum that is captured returns to blowpit 35, then it is pumped to drying system and is dried, add chemistry defoamer to carry out froth breaking without to note therebetween, add chemistry defoamer to carry out froth breaking without to note therebetween.
Six, VC reclaims and removes:
Above-mentioned serum is delivered to serum mixing channel 40 by essence wet crushing mill 36, thin wet crushing mill 36, serum delivery pump 38 from blowpit 35, it is then sent through in VC removing tower 42, reclaim VC monomer further, the VC monomer not being recovered is after Defoaming machine 41 enters gas holder 31, return again to Vinyl Chloride Monomer recycling can 10, seed reactor 24 to be again introduced into and polymerization reaction kettle 29 carry out next course of reaction.
Before vinyl chloride condenses, reclaim vinyl chloride stabilizer and liquid Caustic soda injection treatment；Process together with low oxygen content vinyl chloride, it is to avoid the formation of any vinyl collection polyperoxide；With dosing pump, stabilizer is injected in rectifier unit, with pump, caustic soda is injected in rectifier unit.
VC monomer after recovery, enters and is dried groove 43, to guarantee the conversion of interval and continuous process.
PVC serum, after firing equipment is heated to the temperature controlled, is sent in first order removing tower tower via spray nozzle, is made PVC serum can be suitably distributed over temperature and vacuum in Ta Bishang, and control tower.
Through the oneth VC removing tower 42A removing PVC serum from pipeline at the bottom of tower via being pumped into the 2nd VC removing tower 42B.Before adding the 2nd VC removing tower 42B, PVC serum is heated to control temperature by firing equipment steam；The time of staying of serum is 3～6 hours.PVC serum is through firing equipment (adding thermal medium: steam, spray nozzle send in removing tower 42), and PVC serum can be distributed on the tower wall of first, second VC removing tower 42A, 42B, and the serum time of staying in removing tower 42 is 3～6 hours；Being heated to temperature and control at 50 DEG C～80 DEG C, vacuum degree control is-400～-700mmHg, and after two-stage removes, the content of vinylchloride in serum is down to below 300ppm by about 2000ppm.
Oneth VC removing tower 42A is connected with gas holder 31 by the first Defoaming machine 41, equipped with the first breast by mixing channel 40A between oneth VC removing tower 42A and serum delivery pump 38, equipped with the first vapor removal groove 39A on first serum mixing channel 40A, oneth VC removing tower 42A is connected by the second serum mixing channel 40B and the 2nd VC removing tower 42B, and the 2nd VC removing tower 42B is connected with latex groove 43.
This VC reclaims in removing step, content of vinylchloride in serum is down to below 300ppm by about 2000ppm, has reclaimed VC monomer further, reduces the unit consumption of VC, the VC content in follow-up drying process exhaust outlet emission can be made less than below 10ppm, and package unit is by more environmentally-friendly.
Seven, it is spray-dried, pulverizes:
Serum in dry groove 43 delivers to exsiccator 45 by serum dosing pump 44, resin after being dried enters one-level bag hose 47 and is collected, after being connected with hopper 49 by screen cloth 48 by one section of bag hose 47, deliver in pulverizer 50, after being delivered to two-stage nitration destructor 51 by pulverizer 50 again, being delivered to finished product bin 52 with malleation, finished product bin 52 is connected with automatic packaging system system 53, delivers to warehouse for finished product afterwards.
The pressure control range of malleation conveying: 3000～5000mmH2O；Slurry in spray dryer running is attached to Ta Bishang, can effectively be cleaned up by tower wall via automatic high pressure cleaning equipment.
By using this to be dried, pulverize, positive Pressure Transportation System, fed distance, up to about 200m, can make to be dried, pack and the integral arrangement of finished room is more flexible.
Eight, waste water automatically processes continuously
From storage tank 15, seed reactor 24, polymerization reaction kettle 29, blowpit 35, drying tower 45 discharge wastewater collection waste water collection tank 14, in waste water, VC content is 3000～5000ppm；Waste water is after stripper 7 strips, reclaim and waste water remains VC, VC content is down to below 100ppm, wastewater collection is in waste water equalization basin 6, COD content 2000～3000ppm, SS content 3000～5000ppm, then it is floating except groove 2, (the fast mixed revolution span of control of fast mixed slow mixed groove 4: 80～100 revs/min, slow mixed revolution span of control: 30～50 revs/min to import air Self-pressurizing agri after fast mixed slow mixed groove 4.) automatic scraping sells after collecting into mud cake packaging except the mud concentrated, sludge pumping to the first centrifuge 9 automatic dehydration, dehydration, floating carries out Automatic continuous process except rear waste water delivers to sand filter 1, COD content is down to below 200ppm, then delivers to waste water processing center and process.
The steam injection mode of waste water collection tank 14 is to inject from bottom；The operating condition of steam: temperature 80～98 DEG C, pressure-400～-700mmHg.
By using the continuous automatic processing method of this waste water, reclaim major part residual VC in waste water, VC content is down to below 100ppm by 3000～5000ppm, COD is down to below 200ppm by 2000～3000ppm, SS is down to below 200ppm by 3000～5000ppm, the a whole set of continuous automated processing system of waste water, by DCS control, reduces labor intensity.
Embodiment of the method 2:
The specification of the present embodiment reactor 24 of seed selection selects 35 cubic metres, and the specification of polymerization reaction kettle selects 80 cubic metres.
Apparatus of the present invention are based under security consideration, the reaction of polymerization reaction kettle uses the airtight continuation mode being not turned on manhole cover to carry out in normal service, thus improve the quality of product and production efficiency and safe operation, full production operation process is carried out as follows by DCS control, the concrete technological process of production:
One, prepared by raw material:
1), Vinyl Chloride Monomer is by out-of-bounds delivering in respective VCM monomer preparation tank 11, desalted water is by delivering in hot desalinized water preparation tank 12 outside battery limit (BL), hot desalinized water preparation tank 12 stores 60 DEG C of desalted waters, it is heated to 60 DEG C by being passed through steam, the room temperature desalted water stored in cold desalted water preparation tank 13 is pumped in seed reactor 24 and polymerization reaction kettle 29 by the 5th centrifugal pump 20, and cold desalted water is used for cleaning seed reactor 24 and polymerization reaction kettle 29.
Hot desalinized water is by the 4th centrifugal pumping to seed reactor 24 and polymerization reaction kettle 29.
Additive is prepared by respective storage tank and is stored respectively；Vinyl Chloride Monomer is sent in seed reactor 24 and polymerization reaction kettle 29 as part charging (accounting for Vinyl Chloride Monomer cumulative volume 1/3 ~ 1/6) for the first time.
2), prepared by 200Kg emulsifying agent
Being polymerized of the different trades mark uses different surface action agent:
A-emulsifying agent (EM1), b-emulsifying agent (EM2), c-emulsifying agent (EM3) are for the preparation of emulsion seed and the polymerization of each trade mark, and they are a kind of with water dissolvable thing, be emulsifying agent groove be pre-dissolved be continuously added in seed reactor 24 with in polymerization reaction kettle 29.
3), prepared by 1Kg catalyst
Being pre-dissolved (being also and water-soluble substance) at pre-fluid bowl by the mode similar with emulsifying agent, catalyst AC1 is disposably to add seed reactor 24 by desalted water pipeline with desalted water, and catalyst AC2 disposably adds and in polymerization reaction kettle 29 with desalted water.Catalyst AC1 and catalyst AC2 is respectively 10kg.
4), buffer agent
Two kinds of buffer agents, phosphoric acid about 14kg and Caustic soda 15kg is by with entering to add in seed reactor 24 and polymerization reaction kettle 29, to guarantee that pH value is between 7～8.
5), initiator
The polymerization of the different trades mark uses different initiators, according to the polymerization selection one of the different trades mark:
CAT1, CAT2 are a kind of with water dissolvable peroxide (both are 4kg respectively), be initiator groove be pre-dissolved be continuously added to seed reactor in be first prepared as seed, participate in polyreaction in adding polymerization reaction kettle 29 with seed form the most again.For powder shape, storage form be 25 kilograms packed, storage temperature not can exceed that 27 DEG C.
6), anti-fouling agent
The anti-fouling agent of 4L transfers to anti-fouling agent tank from basin with 0.3～0.9Mpa；Anti-fouling agent is to spray into polymerization reaction kettle by 1.2～2.0Mpa steam jet ejectors, produces fog in polymerization reaction kettle, makes biologically active prod cover all inwalls of reactor.
7), terminator
Under polymerization out-of-control condition, inject 12Kg terminator and terminate course of reaction；Seed reactor 24 and polymerization reaction kettle 29 are equipped with two terminator tanks, all fill terminator solution, and are in 1.6～2.5MPa nitrogen seal pressures.
Two, prepared by seed:
Hot desalinized water about 30 cubic metres, (by the way of heating, desalted water can also be become hot desalinized water) is transported to seed reactor 24 and polymerization reaction kettle 29 by the 4th centrifugal pump 19, emulsifying agent is initially added into when reaction, and other additives pass through pump from storage tank seed injection reactor 24 and polymerization reaction kettle 29.
By initial vacuum pump 32 by polymerization reaction kettle 29 evacuation, when in polymerization reaction kettle 29, pressure is down to 620～680mmHg(0.062 ~ 0.068MPa) time, Vinyl Chloride Monomer is added to polymerization reaction kettle 29 by VCM monomer preparation tank 11；Before adding vinyl chloride, the air in emptying seed reactor 24 and polymerization reaction kettle 29 reactor, when addition accounts for the fresh Vinyl Chloride Monomer of volume ratio 1/3 ~ 1/6, the cumulative volume of Vinyl Chloride Monomer is 35 cubic metres, and polymerization cycle starts.
Time when Seeded polymerization still 29 pressure declines about 0.4Mpa, cooling valve closedown, polymerization terminates；When seed reactor 24 pressure is down to 0.0Mpa, emulsion seed, in filter enters the first seed storage tank 22 and second seed storage tank 23, analyzes size with standby；Size is about between 0.3～0.55 micron.
Afterwards seed reactor 24 inside is carried out quick, safe closed high pressure and automatically clean (high-pressure water pressure 25～35Mpa), DCS control cleaning step.
Cleaning is rinsed with pressure automatic spray in closed after completing again, carries out feeding tube cleaning systems afterwards, carries out the airtight automatic spraying of polymerization reaction kettle 29 anti-adhesion agent afterwards, waits next batch reaction operation；Wherein waste water is unified is collected in waste water collection tank 10.
The temperature operating ranges of seed reactor 24: 45～55 DEG C；The cleaning way of seed reactor 24: closed high pressure cleans automatically, pressure limit: 25～35Mpa.
The spray irrigation mode of seed reactor 24: in closed, pressure is cleaned automatically, pressure limit: 2.5～4.0MPa；Seed reactor 24 anti-adhesion agent spraying method: airtight automatic spraying.
Seed reactor 24 purging system, spray irrigation and anti-adhesion agent spraying all use DCS to control.
Polymerization reaction kettle 29 chuck form: total closed type；The special whipped form of polymerization reaction kettle 29: two-layer SANYE stirs, band baffle plate.
The pressure limit during discharging of polymerization reaction kettle 29: 0.2～0.6Mpa；The cleaning way of polymerization reaction kettle 29: closed high pressure cleans automatically, pressure limit: 25～35Mpa；The spray irrigation mode of polymerization reaction kettle 29: in closed, pressure is cleaned automatically, pressure limit: 2.5～4.0MPa.The anti-adhesion agent spraying method of polymerization reaction kettle 29: airtight automatic spraying.
The cleaning of polymerization reaction kettle 29, spray irrigation and anti-adhesion agent spraying all use DCS to control.
The seed preparation of the application of the invention and post polymerization step, can improve production capacity 50%, reduces labor intensity, it is achieved 45～50 batches are not switched on kettle cover and produce continuously.
Cold desalted water in cold desalted water preparation tank is used for all kinds of grooves and the cleaning of still.
Three, post polymerization:
Hot desalinized water delivers to polymerization reaction kettle 29, and four kinds of additives are simultaneously added polymerization reaction kettle 29, subsequently, emulsion seed is added polymerization reaction kettle 29, then, another part (remove for the first time part add with outer portion) fresh Vinyl Chloride Monomer adds polymerization reaction kettle 29, starts polyreaction；Reaction pressure declines after bulk polymerization speed slows down, and polymerization terminates.
The use of initiator (CAT1 or CAT2 depends on the trade mark), is that the heat discharged by reaction controls；Controlled to add the flow velocity of initiator by the temperature of seed reactor 24 and polymerization reaction kettle 29.
Polymerization reaction kettle 29 is cooled down by total enclosing chuck, and is cooled down by condenser.
For polymerization, only part vinyl chloride is being initially added；Remaining vinyl chloride is to add in polymerization process, and the flow being continuously added to vinyl chloride is to determine according to reaction rate.
Reactor operating condition is different, such as due to the difference of production product grade: when producing the product that the degree of polymerization is 1000, reaction temperature controls at about 45～65 DEG C, and Stress control is at 5～9 kgfs.
Four, storage is reclaimed:
When polymerization reaction kettle pressure is down to 0.2～0.6Mpa, discharge of materials to blowpit 35 reclaims and stores.
Reaction pressure will decline after bulk polymerization speed slows down, and show that polymerization terminates.When polymeric kettle pressure is down to 0.2～0.6Mpa, by discharge of materials to blowpit 35(blowpit 35 slant setting, with the angle that ground exists 5～10 degree) reclaim storage.
Afterwards polymerization reaction kettle 29 inside is carried out enclosed high pressure and automatically clean (high-pressure water pressure 25～35Mpa), DCS control cleaning step.
Cleaning is rinsed with pressure automatic spray in closed after completing again, carries out feeding tube cleaning systems afterwards, carries out the airtight automatic spraying of polymerization reaction kettle 29 anti-adhesion agent afterwards, waits next batch reaction operation；Wherein waste water is unified is collected in waste water collection tank 14.
Five, blowing recovery froth breaking:
Employing negative pressure reclaims, and when the pressure in blowpit 35 is down to 0.2～0.8Mpa, starts discharging and reclaims, and serum carries out defoaming treatment by Defoaming machine；Start vacuum pump and start discharging recovery, until pressure reaches to terminate when-400～-700 in blowpit 35；When blowpit 35 carries out negative pressure recovery, steam is passed directly into blowpit 35 heat up, the pressure limit 0.2～0.5Mpa of steam, serum temperature is made to reach 40 DEG C～80 DEG C, carry out in blowpit in time pushing back receipts and negative pressure recovery (certainly pushing back receipts: the pressure that VCM monomer reaction itself is carried is from blowpit release of pressure), negative pressure reclaims: when in blowpit, the pressure of release of pressure is down to 0.2～0.8Mpa, start vacuum pump to force to extract out, system can take emulsifying agent and the serum that foam includes out of, defoaming treatment is carried out via dynamic defoaming mechanism 34 and static froth breaking mechanism 33, after the serum that is captured returns to blowpit, it is pumped to drying system again be dried, chemistry defoamer is added to carry out froth breaking therebetween without to note, chemistry defoamer is added to carry out froth breaking therebetween without to note.
Six, VC reclaims and removes:
Above-mentioned serum is delivered to serum mixing channel 40 by essence wet crushing mill 36, thin wet crushing mill 36, serum delivery pump 38 from blowpit 35, it is then sent through in VC removing tower 42, reclaim VC monomer further, the VC monomer not being recovered is after Defoaming machine 41 enters gas holder 31, return again to Vinyl Chloride Monomer recycling can 10, seed reactor 24 to be again introduced into and polymerization reaction kettle 29 carry out next course of reaction.
Before vinyl chloride condenses, reclaim vinyl chloride stabilizer and liquid Caustic soda injection treatment；Process together with low oxygen content vinyl chloride, it is to avoid the formation of any vinyl collection polyperoxide；With dosing pump, stabilizer is injected in rectifier unit, with pump, caustic soda is injected in rectifier unit.
VC monomer after recovery, enters and is dried groove 43, to guarantee the conversion of interval and continuous process.
PVC serum, after firing equipment is heated to the temperature controlled, is sent in first order removing tower tower via spray nozzle, is made PVC serum can be suitably distributed over temperature and vacuum in Ta Bishang, and control tower.
Through the oneth VC removing tower 42A removing PVC serum from pipeline at the bottom of tower via being pumped into the 2nd VC removing tower 42B.Before adding the 2nd VC removing tower 42B, PVC serum is heated to control temperature by firing equipment steam；The time of staying of serum is 3～6 hours.PVC serum is through firing equipment (adding thermal medium: steam, spray nozzle send in removing tower 42), and PVC serum can be distributed on the tower wall of first, second VC removing tower 42A, 42B, and the serum time of staying in removing tower 42 is 3～6 hours；Being heated to temperature and control at 50 DEG C～80 DEG C, vacuum degree control is-400～-700mmHg, and after two-stage removes, the content of vinylchloride in serum is down to below 300ppm by about 2000ppm.
Oneth VC removing tower 42A is connected with gas holder 31 by the first Defoaming machine 41, equipped with the first breast by mixing channel 40A between oneth VC removing tower 42A and serum delivery pump 38, equipped with the first vapor removal groove 39A on first serum mixing channel 40A, oneth VC removing tower 42A is connected by the second serum mixing channel 40B and the 2nd VC removing tower 42B, and the 2nd VC removing tower 42B is connected with latex groove 43.
This VC reclaims in removing step, content of vinylchloride in serum is down to below 300ppm by about 2000ppm, has reclaimed VC monomer further, reduces the unit consumption of VC, the VC content in follow-up drying process exhaust outlet emission can be made less than below 10ppm, and package unit is by more environmentally-friendly.
Seven, it is spray-dried, pulverizes:
Serum in dry groove 43 delivers to exsiccator 45 by serum dosing pump 44, resin after being dried enters one-level bag hose 47 and is collected, after being connected with hopper 49 by screen cloth 48 by one section of bag hose 47, deliver in pulverizer 50, after being delivered to two-stage nitration destructor 51 by pulverizer 50 again, being delivered to finished product bin 52 with malleation, finished product bin 52 is connected with automatic packaging system system 53, delivers to warehouse for finished product afterwards.
The pressure control range of malleation conveying: 3000～5000mmH2O；Slurry in spray dryer running is attached to Ta Bishang, can effectively be cleaned up by tower wall via automatic high pressure cleaning equipment.
By using this to be dried, pulverize, positive Pressure Transportation System, fed distance, up to about 200m, can make to be dried, pack and the integral arrangement of finished room is more flexible.
Eight, waste water automatically processes continuously
From storage tank 15, seed reactor 24, polymerization reaction kettle 29, blowpit 35, drying tower 45 discharge wastewater collection waste water collection tank 14, in waste water, VC content is 3000～5000ppm；Waste water is after stripper 7 strips, reclaim and waste water remains VC, VC content is down to below 100ppm, wastewater collection is in waste water equalization basin 6, COD content 2000～3000ppm, SS content 3000～5000ppm, then it is floating except groove 2, (the fast mixed revolution span of control of fast mixed slow mixed groove 4: 80～100 revs/min, slow mixed revolution span of control: 30～50 revs/min to import air Self-pressurizing agri after fast mixed slow mixed groove 4.) automatic scraping sells after collecting into mud cake packaging except the mud concentrated, sludge pumping to the first centrifuge 9 automatic dehydration, dehydration, floating carries out Automatic continuous process except rear waste water delivers to sand filter 1, COD content is down to below 200ppm, then delivers to waste water processing center and process.
The steam injection mode of waste water collection tank 14 is to inject from bottom；The operating condition of steam: temperature 80～98 DEG C, pressure-400～-700mmHg.
By using the continuous automatic processing method of this waste water, reclaim major part residual VC in waste water, VC content is down to below 100ppm by 3000～5000ppm, COD is down to below 200ppm by 2000～3000ppm, SS is down to below 200ppm by 3000～5000ppm, the a whole set of continuous automated processing system of waste water, by DCS control, reduces labor intensity.
The present invention is to be maximized by key equipment polymerization reaction kettle 29 volume, cleans automatization, reclaims without adding chemistry defoamer, tail gas qualified discharge, sewage disposal serialization, increases substantially production capacity, reduce labor intensity, reduces production cost.
The invention is not restricted in above-described embodiment, cited by numerical value, as long as using above-mentioned work technological process, and the polrvinyl chloride seed law that general flow chart based on device is produced sticks with paste resin, within equal apparent is protection scope of the present invention.
Claims (10)
1. the process units sticking with paste resin for the polrvinyl chloride seed law, including preparation tank, storage tank, polymerization reaction kettle, Seeded polymerization still, blowpit, removing tower, drying tower, preparation tank is connected with the top of polymerization reaction kettle and Seeded polymerization still by pipeline respectively, storage tank is connected with seed reactor and polymerization reaction kettle top respectively, and the bottom of seed reactor and polymerization reaction kettle is connected with waste water collection tank respectively；Seed reactor is connected with polymerization reaction kettle top by seed storage tank；It is characterized in that: waste water collection tank is connected with polymerization reaction kettle by stripper and is constituted closed circuit, polymerization reaction kettle bottom is connected with blowpit and removing tower, the export pipeline of blowpit is connected with froth breaking mechanism, and froth breaking mechanism is connected with gas holder after converging with the pipeline of stripper；Removing tower is connected with drying tower, and drying tower is connected with finished product bin by bag hose.
The process units sticking with paste resin for the polrvinyl chloride seed law the most according to claim 1, it is characterised in that: gas holder is connected with vinyl chloride MONOMER RECOVERY tank by rectifier unit, and Vinyl Chloride Monomer recycling can is connected with polymerization reaction kettle.
The process units sticking with paste resin for the polrvinyl chloride seed law the most according to claim 1, it is characterised in that: preparation tank is divided into Vinyl Chloride Monomer preparation tank, hot desalinized water preparation tank and cold desalted water preparation tank；Aforementioned three preparation tanks are connected with seed reactor and polymerization reaction kettle respectively.
The process units sticking with paste resin for the polrvinyl chloride seed law the most according to claim 1, it is characterized in that: stripper is connected with equalization basin, equalization basin is connected with measuring tank, measuring tank is connected with fast mixed slow mixed groove, fast mixed slow mixed groove is connected with neutralization chamber, neutralization chamber is connected with the floating groove that removes, and the floating groove that removes is connected with sand filter and centrifuge respectively.
The process units sticking with paste resin for the polrvinyl chloride seed law the most according to claim 1, it is characterised in that: storage tank is divided into four kinds, is emulsifying agent storage tank, catalyst storage tank, initiator storage tank and buffer agent storage tank respectively.
The process units sticking with paste resin for the polrvinyl chloride seed law the most according to claim 1, it is characterised in that: blowpit passes sequentially through dynamic defoaming mechanism, static froth breaking mechanism is connected with gas holder.
The process units sticking with paste resin for the polrvinyl chloride seed law the most according to claim 1, it is characterised in that: blowpit is connected with VC removing tower by wet crushing mill, serum delivery pump.
The process units sticking with paste resin for the polrvinyl chloride seed law the most according to claim 1, it is characterised in that: VC removing tower is connected with drying tower by latex groove.
The process units sticking with paste resin for the polrvinyl chloride seed law the most according to claim 1, it is characterised in that: drying tower passes sequentially through one-level bag hose, hopper, pulverizer, two grades of bag hoses are connected with finished product bin, and finished product bin is connected with automatic packaging system.
The process units sticking with paste resin for the polrvinyl chloride seed law the most according to claim 1, it is characterized in that: seed reactor and polymerization reaction kettle are stainless steel cauldron, the volume of seed reactor at 30～55 cubic metres, polymerization reaction kettle and volume at 65～90 cubic metres.
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| CN201620277564.4U CN205420252U (en) | 2016-04-06 | 2016-04-06 | A apparatus for producing for polyvinyl chloride seed law paste resin |
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| CN201620277564.4U CN205420252U (en) | 2016-04-06 | 2016-04-06 | A apparatus for producing for polyvinyl chloride seed law paste resin |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107141386A (en) * | 2017-06-16 | 2017-09-08 | 唐山三友氯碱有限责任公司 | A kind of method for producing PVC paste resin and reaction retracting device |
| CN112812206A (en) * | 2021-02-25 | 2021-05-18 | 华阳新材料科技集团有限公司 | Device and method for producing polyvinyl chloride by multi-kettle continuous polymerization |
-
2016
- 2016-04-06 CN CN201620277564.4U patent/CN205420252U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107141386A (en) * | 2017-06-16 | 2017-09-08 | 唐山三友氯碱有限责任公司 | A kind of method for producing PVC paste resin and reaction retracting device |
| CN112812206A (en) * | 2021-02-25 | 2021-05-18 | 华阳新材料科技集团有限公司 | Device and method for producing polyvinyl chloride by multi-kettle continuous polymerization |
| CN112812206B (en) * | 2021-02-25 | 2024-03-19 | 华阳新材料科技集团有限公司 | Device and method for producing polyvinyl chloride by multi-kettle continuous polymerization |
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