CN114716594B - Production method of polyvinyl chloride resin - Google Patents
Production method of polyvinyl chloride resin Download PDFInfo
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- CN114716594B CN114716594B CN202210380406.1A CN202210380406A CN114716594B CN 114716594 B CN114716594 B CN 114716594B CN 202210380406 A CN202210380406 A CN 202210380406A CN 114716594 B CN114716594 B CN 114716594B
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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
- C08F2/002—Scale prevention in a polymerisation reactor or its auxiliary parts
- C08F2/004—Scale prevention in a polymerisation reactor or its auxiliary parts by a prior coating on the reactor walls
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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
- C08F2/44—Polymerisation in the presence of compounding ingredients, e.g. plasticisers, dyestuffs, fillers
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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
- C08F4/00—Polymerisation catalysts
- C08F4/28—Oxygen or compounds releasing free oxygen
- C08F4/32—Organic compounds
- C08F4/38—Mixtures of peroxy-compounds
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08K—Use of inorganic or non-macromolecular organic substances as compounding ingredients
- C08K3/00—Use of inorganic substances as compounding ingredients
- C08K3/18—Oxygen-containing compounds, e.g. metal carbonyls
- C08K3/24—Acids; Salts thereof
- C08K3/26—Carbonates; Bicarbonates
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Abstract
The invention relates to the technical field of polyvinyl chloride resin production, in particular to a production method of polyvinyl chloride resin, which is carried out according to the following steps: the method comprises the steps of adopting an anti-sticking agent to coat a kettle, adding an inefficient buffering agent into the polymerization kettle under the condition of stirring, synchronously adding desalted water and polyethylene monomer into the polymerization kettle, simultaneously adding a dispersing agent into the polymerization kettle, adding an initiator into the polymerization kettle after the desalted water and the polyethylene monomer are added, carrying out polymerization reaction in the polymerization kettle, and adding a terminator into the polymerization kettle after the polymerization reaction is finished to obtain the polyvinyl chloride resin. The production method of the polyvinyl chloride resin can produce the polyvinyl chloride resin with good stability and better particle morphology under a 137m polymerization kettle system, simultaneously reduces the use of auxiliary agents, lowers the production cost and lowers the difficulty of sewage treatment.
Description
Technical Field
The invention relates to the technical field of polyvinyl chloride resin production, in particular to a production method of polyvinyl chloride resin.
Background
The polymerization kettle is a 137 m-sized polymerization kettle produced by Liaoning Korea chemical industry group and is the largest domestic polymerization kettle, the polymerization kettle refers to a Goldrich polymerization process, and the polyvinyl chloride resin with excellent indexes is produced under the actions of a ternary dispersion system, a composite binary initiation system and a buffering agent (comprising an inefficient buffering agent and a high-efficient buffering agent) by adopting an isothermal water feeding process, but in the actual production process, the auxiliary agent consumption is high, the industrial competitive advantage is not obvious, the centrifugal mother liquor produced by the downstream process is difficult to treat, the recycling value is low, and the wastewater treatment cost is high.
Disclosure of Invention
The invention provides a production method of polyvinyl chloride resin, which overcomes the defects of the prior art, and can effectively solve the problems of high auxiliary agent consumption and difficult wastewater treatment in the existing polyvinyl chloride resin production process.
The technical scheme of the invention is realized by the following measures: a production method of polyvinyl chloride resin is carried out according to the following steps: coating a kettle by adopting an anti-sticking kettle agent, adding an inefficient buffering agent into the polymerization kettle under the condition of stirring, synchronously adding desalted water and vinyl chloride monomer into the polymerization kettle, simultaneously adding a dispersing agent into the polymerization kettle, adding an initiator into the polymerization kettle after the desalted water and the vinyl chloride monomer are added, carrying out polymerization reaction in the polymerization kettle, and adding a terminator into the polymerization kettle after the polymerization reaction is finished to obtain the polyvinyl chloride resin; the raw materials comprise, by weight, 12 to 16 parts of anti-sticking agent, 8 to 12 parts of low-efficiency buffer, 52.0 to 52.2 parts of dispersing agent, 28.3 to 28.7 parts of initiator, 58 to 62 parts of terminator, 56000 to 58000 parts of desalted water and 48000 to 50000 parts of vinyl chloride monomer.
The following are further optimizations and/or improvements to the above-described inventive solution:
the dispersing agent comprises the following components in percentage by weight: 1:1.4 to 1.5 of a first dispersing agent, a second dispersing agent and a third dispersing agent, wherein the first dispersing agent is polyvinyl alcohol with the mass concentration of 78%, the second dispersing agent is hydroxypropyl methyl cellulose ether, the third dispersing agent is polyvinyl alcohol with the mass concentration of 45%, the adding sequence of the dispersing agents is that the polyvinyl alcohol with the mass concentration of 78% and the polyvinyl alcohol with the mass concentration of 45% are firstly added, and then the hydroxypropyl methyl cellulose ether is added.
The weight ratio of the initiator is 4.5 to 4.6:1 bis (2-ethylhexyl) peroxydicarbonate (EHP) and cumyl peroxyneodecanoate (CNP).
The low-efficiency buffer is ammonium bicarbonate.
The polymerization temperature is 56.7+/-0.5 ℃, the pressure is 0.70MPa to 0.95MPa, and the polymerization time is 250min to 270min.
In the polymerization reaction, the pH of the mixture in the kettle is maintained between 7.5 and 8.5.
The production method of the polyvinyl chloride resin can produce the polyvinyl chloride resin with good stability and better particle morphology under a 137m polymerization kettle system, simultaneously reduces the use of auxiliary agents, lowers the production cost and lowers the difficulty of sewage treatment.
Detailed Description
The present invention is not limited by the following examples, and specific embodiments can be determined according to the technical scheme and practical situations of the present invention. The various chemical reagents and chemical supplies mentioned in the invention are all commonly known and used in the prior art unless specified otherwise; the percentages in the invention are mass percentages unless otherwise specified.
The invention is further described below with reference to examples:
example 1: the production method of the polyvinyl chloride resin is carried out according to the following steps: coating a kettle by adopting an anti-sticking kettle agent, adding an inefficient buffering agent into the polymerization kettle under the condition of stirring, synchronously adding desalted water and vinyl chloride monomer into the polymerization kettle, simultaneously adding a dispersing agent into the polymerization kettle, adding an initiator into the polymerization kettle after the desalted water and the vinyl chloride monomer are added, carrying out polymerization reaction in the polymerization kettle, and adding a terminator into the polymerization kettle after the polymerization reaction is finished to obtain the polyvinyl chloride resin; the raw materials comprise, by weight, 12 to 16 parts of anti-sticking agent, 8 to 12 parts of low-efficiency buffer, 52.0 to 52.2 parts of dispersing agent, 28.3 to 28.7 parts of initiator, 58 to 62 parts of terminator, 56000 to 58000 parts of desalted water and 48000 to 50000 parts of vinyl chloride monomer.
In the existing polyvinyl chloride resin production process, the pH value of the whole system needs to be controlled through low-efficiency buffer ammonium bicarbonate and high-efficiency buffer sodium hydroxide, after the low-efficiency buffer ammonium bicarbonate (added before polymerization) and the high-efficiency buffer sodium hydroxide (added after 90min of polymerization) are added, the system can gradually develop alkalinity in the whole polymerization kettle reaction process, and before and after the terminator is added, the pH value can reach 8.5 to 9.5, even higher, so that the treatment of mother liquor water is not facilitated.
The production method of polyvinyl chloride resin is improved on the basis of the prior art, the high-efficiency buffer sodium hydroxide is omitted in the formula, only the low-efficiency buffer ammonium bicarbonate is adopted, and the pH value of a reaction system of a polymerization kettle is controlled to be maintained between 6 and 9. In the production process of polyvinyl chloride resin, the data of a plurality of tests show that the requirement of the reaction system in the reactor on the pH value can be met without adding high-efficiency buffer sodium hydroxide in the polymerization reaction process in the polymerization reactor. The quality of the product obtained after improvement is unchanged, the low-efficiency buffer sodium hydroxide is cancelled in the formula, the product quality is not influenced, the problem of high consumption of auxiliary agents is solved, the product competitiveness is improved, meanwhile, after the high-efficiency buffer sodium hydroxide is cancelled, the pH value of mother liquor water is maintained at 7.8-8.5, the requirements of wastewater treatment and recycling are met, and the difficulty of wastewater treatment is reduced.
Before the improvement of the invention: 1. the pH value of the mother liquor water is high, and the mother liquor water is alkaline, so that the sewage treatment is not facilitated; 2. when alkali is added into the polymerization kettle, the on-site operation risk is increased, meanwhile, the on-site safety management is inconvenient, sodium hydroxide belongs to dangerous chemicals, the management difficulty is high, and the safety coefficient is low; 3. the polymerization system is unstable, the dispersant system is easy to be destroyed due to the fluctuation of the pH value of the system, the resin screening is affected, and particles are produced when serious.
After the improvement of the invention: 1. the addition of the high-efficiency buffer NaOH in the polymerization reaction is omitted, and under the condition of keeping the original resin product quality unchanged, the auxiliary agent is saved, and the production cost of the resin is reduced; 2. the pH value of the mother liquor is reduced, and the difficulty of sewage treatment is reduced; 3. after NaOH is canceled from being added, the difficulty of on-site operation analysis and hazardous chemical substance management is reduced; 4. the pH value of the polymerization system is more stable, the quality of the polyvinyl chloride resin product is more stable, and the particle morphology of the polyvinyl chloride resin is better.
In the invention, the anti-sticking agent adopts the existing well-known and common anti-sticking agent or adopts the anti-sticking agent with the model number HTL-10 provided by Xinjiang Huatailong chemical auxiliary agent, and the terminator adopts the existing well-known and common terminator or adopts the terminator with the model number TR-10 provided by Xinjiang Huatailong chemical auxiliary agent.
Example 2: as an optimization of the above examples, the dispersant comprises 3:1:1.4 to 1.5 of a first dispersing agent, a second dispersing agent and a third dispersing agent, wherein the first dispersing agent is polyvinyl alcohol with the mass concentration of 78%, the second dispersing agent is hydroxypropyl methyl cellulose ether, the third dispersing agent is polyvinyl alcohol with the mass concentration of 45%, the adding sequence of the dispersing agents is that the polyvinyl alcohol with the mass concentration of 78% and the polyvinyl alcohol with the mass concentration of 45% are firstly added, and then the hydroxypropyl methyl cellulose ether is added.
Example 3: as an optimization of the above examples, the initiator weight ratio was 4.5 to 4.6:1 bis (2-ethylhexyl) peroxydicarbonate (EHP) and cumyl peroxyneodecanoate (CNP).
Example 4: as an optimization of the above embodiment, the inefficient buffer is ammonium bicarbonate.
Example 5: as an optimization of the above examples, the polymerization temperature was 56.7deg.C.+ -. 0.5 ℃, the pressure was 0.70MPa to 0.95MPa, and the polymerization time was 250min to 270min.
Example 6: as optimization of the above examples, the pH of the mixture in the reactor was maintained between 7.5 and 8.5 during the polymerization reaction.
Example 7: the production method of the polyvinyl chloride resin is carried out according to the following steps: coating a kettle by adopting an anti-sticking kettle agent, adding ammonium bicarbonate into the polymerization kettle under the condition of stirring, synchronously adding desalted water and vinyl chloride monomer into the polymerization kettle, simultaneously adding a dispersing agent into the polymerization kettle, adding an initiator into the polymerization kettle after the desalted water and the vinyl chloride monomer are added, carrying out polymerization reaction in the polymerization kettle, and adding a terminator into the polymerization kettle after the polymerization reaction is finished to obtain the polyvinyl chloride resin; the raw materials comprise 12 parts of anti-sticking agent, 8 parts of ammonium bicarbonate, 52.0 parts of dispersing agent, 28.3 parts of initiator, 58 parts of terminator, 56000 parts of desalted water and 48000 parts of vinyl chloride monomer according to parts by weight. Wherein the dispersing agent comprises the following components in percentage by weight: 1:1.4, a first dispersing agent, a second dispersing agent and a third dispersing agent, wherein the first dispersing agent is polyvinyl alcohol with the mass concentration of 78%, the second dispersing agent is hydroxypropyl methyl cellulose ether, the third dispersing agent is polyvinyl alcohol with the mass concentration of 45%, and the adding sequence of the dispersing agents is polyvinyl alcohol with the mass concentration of 78%, polyvinyl alcohol with the mass concentration of 45% and hydroxypropyl methyl cellulose ether in sequence; the weight ratio of the initiator is 4.5:1 bis (2-ethylhexyl) peroxydicarbonate (EHP) and cumyl peroxyneodecanoate (CNP); the polymerization temperature was 56.2℃and the pressure was 0.70MPa, the polymerization time was 250 minutes, and the pH of the mixed solution in the autoclave was 7.5.
Example 8: the production method of the polyvinyl chloride resin is carried out according to the following steps: coating a kettle by adopting an anti-sticking kettle agent, adding ammonium bicarbonate into the polymerization kettle under the condition of stirring, synchronously adding desalted water and vinyl chloride monomer into the polymerization kettle, simultaneously adding a dispersing agent into the polymerization kettle, adding an initiator into the polymerization kettle after the desalted water and the vinyl chloride monomer are added, carrying out polymerization reaction in the polymerization kettle, and adding a terminator into the polymerization kettle after the polymerization reaction is finished to obtain the polyvinyl chloride resin; the raw materials comprise, by weight, 16 parts of anti-sticking agent, 12 parts of ammonium bicarbonate, 52.2 parts of dispersing agent, 28.7 parts of initiator, 62 parts of terminator, 58000 parts of desalted water and 50000 parts of vinyl chloride monomer. Wherein the dispersing agent comprises the following components in percentage by weight: 1:1.5, a first dispersing agent, a second dispersing agent and a third dispersing agent, wherein the first dispersing agent is polyvinyl alcohol with the mass concentration of 78%, the second dispersing agent is hydroxypropyl methyl cellulose ether, the third dispersing agent is polyvinyl alcohol with the mass concentration of 45%, and the dispersing agents are sequentially added in the order of 45% polyvinyl alcohol, 78% polyvinyl alcohol and hydroxypropyl methyl cellulose ether; the weight ratio of the initiator is 4.6:1 bis (2-ethylhexyl) peroxydicarbonate (EHP) and cumyl peroxyneodecanoate (CNP); the polymerization temperature was 57.2℃and the pressure was 0.95MPa, the polymerization time was 270min, and the pH of the mixed solution in the autoclave was 8.5.
Example 9: the production method of the polyvinyl chloride resin is carried out according to the following steps: coating a kettle by adopting an anti-sticking kettle agent, adding ammonium bicarbonate into the polymerization kettle under the condition of stirring, synchronously adding desalted water and vinyl chloride monomer into the polymerization kettle, simultaneously adding a dispersing agent into the polymerization kettle, adding an initiator into the polymerization kettle after the desalted water and the vinyl chloride monomer are added, carrying out polymerization reaction in the polymerization kettle, and adding a terminator into the polymerization kettle after the polymerization reaction is finished to obtain the polyvinyl chloride resin; the raw materials comprise 14 parts of anti-sticking agent, 10 parts of ammonium bicarbonate, 52.1 parts of dispersing agent, 28.5 parts of initiator, 6 parts of terminator, 57000 parts of desalted water and 49000 parts of vinyl chloride monomer according to parts by weight. Wherein the dispersing agent comprises the following components in percentage by weight: 1:1.45 of a first dispersing agent, a second dispersing agent and a third dispersing agent, wherein the first dispersing agent is polyvinyl alcohol with the mass concentration of 78%, the second dispersing agent is hydroxypropyl methyl cellulose ether, the third dispersing agent is polyvinyl alcohol with the mass concentration of 45%, and the adding sequence of the dispersing agents is polyvinyl alcohol with the mass concentration of 78%, polyvinyl alcohol with the mass concentration of 45% and hydroxypropyl methyl cellulose ether in sequence; the weight ratio of the initiator is 4.55:1 bis (2-ethylhexyl) peroxydicarbonate (EHP) and cumyl peroxyneodecanoate (CNP); the polymerization temperature is 57.0 ℃, the pressure is 0.80MPa, the polymerization time is 260min, and the pH value of the mixed solution in the kettle is 8.0.
Example 10: the production method of the polyvinyl chloride resin is carried out according to the following steps: coating a kettle by adopting an anti-sticking kettle agent, adding ammonium bicarbonate into the polymerization kettle under the condition of stirring, synchronously adding desalted water and vinyl chloride monomer into the polymerization kettle, sequentially adding a dispersing agent I, a dispersing agent III and a dispersing agent II into the polymerization kettle while synchronously adding the desalted water and the vinyl chloride monomer, adding an initiator into the polymerization kettle after the desalted water and the vinyl chloride monomer are added, and adding a terminator into the polymerization kettle after the polymerization reaction is finished to obtain the polyvinyl chloride resin; wherein the polymerization kettle adopts 137m 3 The adding amount (kg) of the single kettle raw materials comprises 14kg of anti-sticking agent, 10kg of ammonium bicarbonate, 28.5kg of dispersing agent I, 9.5kg of dispersing agent II, 14.1kg of dispersing agent III, 28.5kg of initiator, 60kg of terminator, 57000kg of desalted water and 49000kg of vinyl chloride monomer. Wherein the first dispersing agent is polyvinyl alcohol with the mass concentration of 78%, the second dispersing agent is hydroxypropyl methyl cellulose ether, and the third dispersing agent is polyvinyl alcohol with the mass concentration of 45%; the initiator was mixed from 23.38kg of di (2-ethylhexyl) peroxydicarbonate (EHP) and 5.12kg of cumyl peroxyneodecanoate (CNP); the polymerization temperature was 56.2℃and the pressure was 0.70MPa, the polymerization time was 250 minutes, and the pH of the mixed solution in the autoclave was maintained at 8.0.
Example 11: the procedure of example 10 was repeated except that the polymerization temperature was changed to 56.2℃and the pressure was 0.70MPa and the polymerization time was 250min, and the polymerization temperature was 57.2℃and the pressure was 0.95MPa and the polymerization time was 270min.
Example 12: the procedure of example 10 was repeated except that the polymerization temperature was changed to 56.2℃and the pressure was 0.70MPa and the polymerization time was 250min, and the polymerization temperature was 57.0℃and the pressure was 0.80MPa and the polymerization time was 260 min.
Comparative example 1: in example 10 of the present invention, the procedure was the same as in example 10 except that ammonium bicarbonate (single pot addition amount: 10 kg) was added to the polymerization vessel instead of ammonium bicarbonate (single pot addition amount: 6 kg) and sodium hydroxide (single pot addition amount: 1.2 kg) was added after 90 minutes of polymerization.
Comparative example 2: in example 11 of the present invention, ammonium bicarbonate (single pot addition amount: 10 kg) was added to the polymerization pot instead of ammonium bicarbonate (single pot addition amount: 6 kg) and sodium hydroxide (single pot addition amount: 1.2 kg) were added after 90 minutes of polymerization, and the other steps were the same as in example 11.
Comparative example 3: in example 12 of the present invention, ammonium bicarbonate (single pot addition amount: 10 kg) was added to the polymerization pot instead of ammonium bicarbonate (single pot addition amount: 6 kg) and sodium hydroxide (single pot addition amount: 1.2 kg) were added after 90 minutes of polymerization, and the other steps were the same as in example 12.
Comparative example 4: in example 12 of the present invention, ammonium bicarbonate (single pot addition amount: 10 kg) was added to the polymerization pot instead of ammonium bicarbonate (single pot addition amount: 6 kg) and sodium hydroxide (single pot addition amount: 4 kg) were added after 90 minutes of polymerization, and the other steps were the same as in example 12.
The polyvinyl chloride resins prepared by the production methods of the polyvinyl chloride resins prepared in examples 7 to 12 of the present invention have good stability and better particle morphology, and the properties of the polyvinyl chloride resins obtained in examples 10 to 12 of the present invention are examined below.
The properties of the polyvinyl chloride resins obtained in examples 10 to 12 of the present invention were examined in "general polyvinyl chloride resin by suspension method", and the detection indexes include: the test method comprises the following steps: the polyvinyl chloride resins obtained in comparative examples 1 to 4 of the present invention were used as a comparative example while referring to GB/T5761-2018 viscosity, impurity particle count, volatiles, thermostability, 63 μm screen residue, fish eye count, whiteness, residue, apparent density, 250 μm screen residue, oil absorption and particle size distribution.
Test results: the properties of the polyvinyl chloride resins obtained in comparative examples 1 to 4 are shown in tables 1 and 2, the properties of the polyvinyl chloride resins obtained in examples 10 to 12 are shown in tables 3 and 4, and in the detection indexes, compared with the polyvinyl chloride resins obtained in comparative examples 1 to 4, the polyvinyl chloride resins obtained in examples 10 to 12 have higher oil absorption and lower 250 μm screen residues, indicating that the polyvinyl chloride resins prepared by the production method of the polyvinyl chloride resins of the invention have better stability; the polyvinyl chloride resins obtained in examples 10 to 12 of the present invention were different in particle size distribution (120 mesh/0.12 mm, 140 mesh/0.109 mm, 160 mesh/0.096 mm, 180 mesh/0.8 mm and 200 mesh/0.075 mm) and superior to the polyvinyl chloride resins obtained in comparative examples 1 to 4 of the present invention, indicating that the morphology of the polyvinyl chloride resin particles prepared by the production method of the polyvinyl chloride resin of the present invention was better.
In conclusion, the production method of the polyvinyl chloride resin can produce the polyvinyl chloride resin with good stability and better particle morphology under a 137m polymerization kettle system, and simultaneously, the use of auxiliary agents is reduced, the production cost is reduced, and the difficulty of sewage treatment is reduced.
The technical characteristics form the embodiment of the invention, have stronger adaptability and implementation effect, and can increase or decrease unnecessary technical characteristics according to actual needs so as to meet the requirements of different situations.
Claims (3)
1. The production method of the polyvinyl chloride resin is characterized by comprising the following steps: coating a kettle by adopting an anti-sticking kettle agent, adding an inefficient buffering agent into the polymerization kettle under the condition of stirring, synchronously adding desalted water and vinyl chloride monomer into the polymerization kettle, simultaneously adding a dispersing agent into the polymerization kettle, adding an initiator into the polymerization kettle after the desalted water and the vinyl chloride monomer are added, carrying out polymerization reaction in the polymerization kettle, and adding a terminator into the polymerization kettle after the polymerization reaction is finished to obtain the polyvinyl chloride resin; wherein the raw materials comprise, by weight, 12 to 16 parts of anti-sticking agent, 8 to 12 parts of low-efficiency buffer, 52.0 to 52.2 parts of dispersant, 28.3 to 28.7 parts of initiator, 58 to 62 parts of terminator, 56000 to 58000 parts of desalted water and 48000 to 50000 parts of vinyl chloride monomer; wherein the dispersing agent comprises the following components in percentage by weight: 1:1.4 to 1.5 of a first dispersing agent, a second dispersing agent and a third dispersing agent, wherein the first dispersing agent is polyvinyl alcohol with the mass concentration of 78%, the second dispersing agent is hydroxypropyl methyl cellulose ether, the third dispersing agent is polyvinyl alcohol with the mass concentration of 45%, the adding sequence of the dispersing agents is that the polyvinyl alcohol with the mass concentration of 78% and the polyvinyl alcohol with the mass concentration of 45% are firstly added, and then the hydroxypropyl methyl cellulose ether is added; during polymerization, the pH of the mixed solution in the kettle is maintained between 7.5 and 8.5.
2. The method for producing polyvinyl chloride resin according to claim 1, wherein the low-efficiency buffer is ammonium bicarbonate.
3. The method for producing a polyvinyl chloride resin according to claim 1 or 2, wherein the polymerization temperature is 56.7 ℃ ± 0.5 ℃, the pressure is 0.70MPa to 0.95MPa, and the polymerization time is 250min to 270min.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106749795A (en) * | 2016-07-17 | 2017-05-31 | 佛山瑞箭体育器材有限公司 | A kind of preparation method of Corvic |
| CN110078851A (en) * | 2019-04-29 | 2019-08-02 | 杰瑞德工业设备(北京)有限公司 | Polyvinyl chloride suspension polymerization |
| CN111393548A (en) * | 2020-04-13 | 2020-07-10 | 内蒙古鄂尔多斯电力冶金集团股份有限公司 | Preparation method of polyvinyl chloride resin with high thermal stability |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106749795A (en) * | 2016-07-17 | 2017-05-31 | 佛山瑞箭体育器材有限公司 | A kind of preparation method of Corvic |
| CN110078851A (en) * | 2019-04-29 | 2019-08-02 | 杰瑞德工业设备(北京)有限公司 | Polyvinyl chloride suspension polymerization |
| CN111393548A (en) * | 2020-04-13 | 2020-07-10 | 内蒙古鄂尔多斯电力冶金集团股份有限公司 | Preparation method of polyvinyl chloride resin with high thermal stability |
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