阅读说明：本技术 一种聚苯硫醚生产中苯硫醚齐聚物的回收方法 (Method for recovering phenylene sulfide oligomer in polyphenylene sulfide production ) 是由 廖斌 张定明 刘勇 于 2019-11-18 设计创作，主要内容包括：本发明涉及聚苯硫醚副产物回收技术领域,具体涉及一种聚苯硫醚生产中苯硫醚齐聚物的回收方法。具体方案为：一种聚苯硫醚生产中苯硫醚齐聚物的回收方法,对合成料浆液进行固液分离,分离的滤液进行减压蒸发,蒸发后剩余的滤液与冲洗水和配将水进行混合,然后经过滤、蒸发、过滤、二次洗涤、二次过滤后得到苯硫醚齐聚物。本发明在现有的工艺流程和设备基础上,对现有的聚合物合成料浆液回收工艺进行优化,从而达到工艺流程更短,缩短生产周期,降低能耗的生产目标,保障了生产的连续化和中间废产物资源的循环源再利用,有效的解决了废渣等环保相关问题。(The invention relates to the technical field of polyphenylene sulfide byproduct recovery, in particular to a method for recovering a phenylene sulfide oligomer in polyphenylene sulfide production. The specific scheme is as follows: a process for recovering the oligomer of diphenyl sulfide includes such steps as solid-liquid separation of resultant slurry, vacuum evaporation of separated filtrate, mixing the residual filtrate with flushing water and water, filtering, evaporating, filtering, washing and filtering again. The invention optimizes the existing polymer synthetic material slurry recovery process on the basis of the existing process flow and equipment, thereby achieving the production aims of shortening the process flow, shortening the production period and reducing the energy consumption, ensuring the continuity of production and the recycling source reutilization of intermediate waste product resources, and effectively solving the environmental protection related problems of waste residues and the like.)

1. A method for recovering a phenylene sulfide oligomer in the production of polyphenylene sulfide is characterized by comprising the following steps: the method comprises the following steps:

(1) carrying out solid-liquid separation on the synthetic material slurry after the polymerization reaction, washing and drying a filter cake obtained by separation to obtain PPS, and recovering mixed water generated by recovering the PPS into a mixed water storage tank for later use; adding the separated filtrate into an evaporator for reduced pressure evaporation, and adding the residual filtrate into an oligomer extraction tank for later use;

(2) adding the mixed water obtained in the step (1) into an oligomer extraction tank, stirring the mixed water and the residual filtrate to obtain a mixed solution, and then conveying the mixed solution to a first-stage plate-and-frame filter for filtering;

(3) recycling the filter cake collected after the filtration of the first-stage plate and frame filter in the step (2) into a fine powder storage tank, mixing the filter cake with the PPS in the step (1) to obtain a mixture, adding hot water, stirring uniformly, conveying the mixture to the first-stage plate and frame filter for secondary filtration, drying the filter cake collected after the filtration, recycling, and conveying the filtrate obtained after the first filtration of the first-stage plate and frame filter to the second-stage plate and frame filter for filtration;

(4) recovering the filter cake collected after the filtration by the second-stage plate-and-frame filter in the step (3) into a low polymer storage tank, adding hot water, uniformly stirring, conveying to the second-stage plate-and-frame filter, filtering again to obtain a semi-finished product of the diphenyl sulfide oligomer, and drying the filter cake in vacuum to obtain the diphenyl sulfide oligomer; and (4) carrying out the next salt recovery process on the filtrate obtained after the first filtration of the second-stage plate-and-frame filter.

2. The method for recovering the diphenyl sulfide oligomer in the production of polyphenylene sulfide as claimed in claim 1, wherein: in the step (1), the temperature of the synthetic material slurry is 70-90 ℃.

3. The method for recovering the diphenyl sulfide oligomer in the production of polyphenylene sulfide as claimed in claim 1, wherein: and (2) in the step (1), washing, purifying, preparing slurry, centrifugally separating and drying the separated filter cake to obtain PPS, and recycling mixed water of washing water and slurry preparing water generated in the washing and slurry preparing processes into a mixed water storage tank for later use.

4. The method for recovering the diphenyl sulfide oligomer in the production of polyphenylene sulfide as claimed in claim 1, wherein: in the step (1), the adding amount of the filtrate is 60-70% of the volume of the evaporator, the vacuum degree of the evaporator is-0.05-0.08 MPa, the temperature is 90-140 ℃, and the rotating speed is 80-120 rmp/min.

5. The method for recovering the diphenyl sulfide oligomer in the production of polyphenylene sulfide as claimed in claim 1, wherein: in the step (1), after the filtrate is evaporated under reduced pressure, the volume of the residual filtrate is 20-25% of the volume of the filtrate before evaporation, and when the mass of the residual solvent NMP in the residual filtrate is 20-30%, the reduced pressure evaporation of the filtrate is stopped.

6. The method for recovering the diphenyl sulfide oligomer in the production of polyphenylene sulfide as claimed in claim 1, wherein: in the step (1), the solvent NMP is obtained by condensing the gas phase obtained after the filtrate is evaporated under reduced pressure and recovering.

7. The method for recovering the diphenyl sulfide oligomer in the production of polyphenylene sulfide as claimed in claim 1, wherein: in the step (2), the rotating speed of the oligomer extraction tank is 40-60 rpm/min, the temperature is 60-80 ℃, and the stirring time is 10-15 min.

8. The method for recovering the diphenyl sulfide oligomer in the production of polyphenylene sulfide as claimed in claim 5, wherein: in the step (2), the mass ratio of the mixed water to the residual solvent NMP in the residual filtrate is 8-10: 1.

9. The method for recovering the diphenyl sulfide oligomer in the production of polyphenylene sulfide as claimed in claim 1, wherein: in the step (3), the temperature of the hot water is 50-60 ℃, and the mass ratio of the mixture to the hot water is 1: 2-3.

10. The method for recovering the diphenyl sulfide oligomer in the production of polyphenylene sulfide as claimed in claim 1, wherein: in the step (4), the vacuum degree of vacuum drying is-0.05 to-0.08 Mpa, and the temperature is 80 to 90 ℃.

Technical Field

The invention relates to the technical field of polyphenylene sulfide byproduct recovery, in particular to a method for recovering a phenylene sulfide oligomer in polyphenylene sulfide production.

Background

Polyphenylene sulfide (hereinafter abbreviated as PPS) resin has been rapidly developed in recent years as an engineering plastic having an optimum cost performance. Was first developed by philips oil company in 1967 and put into commercial production in 1973. The main production principle is that p-dichlorobenzene and sodium sulfide are synthesized by pressure polycondensation in N-methylpyrrolidone (NMP) solution, and after the expiration of the patent of Phillips Petroleum company in 1984, European and Japanese companies and the like develop respective process routes on the basis of the pressure polycondensation, but the production principle is almost similar to the initial patent of Phillips and is based on the polycondensation of aromatic nucleophilic reaction to generate sodium chloride. The method has the characteristics of low raw material cost, controllable reaction, high resin linearity and the defects of large solvent amount circulation amount of a reaction system (6 tons of solvent are needed for producing 1 ton of resin), more byproducts (the content is 3-5%) in polymerization reaction, enrichment in the solvent and residue in a finished product, thereby influencing the product quality and equipment pipeline blockage, having low operation efficiency, large solvent loss (1 ton of product consumes about 1 ton of solvent), seriously prolonging the production period, having high production cost, and causing a series of problems that a large amount of waste residues generated in the production process are difficult to treat in an environment-friendly way, and the like, thereby becoming a bottleneck for the development of domestic PPS industrial production.

At present, 1/3 patent is published in the related PPS patent documents, which relates to the optimization of raw materials, solvents, catalytic systems and partial process flows for production, such as Japanese Imperial corporation for the manufacturing method of polyphenylene sulfide fibers; dongli corporation "manufacturing method of aromatic sulfide fiber" and "manufacturing method of polyphenylene sulfite monofilament", in China, patent applications for polyphenylene sulfide synthesis were first filed by Sichuan university to the intellectual property office in China (a method for synthesizing high molecular weight linear polyphenylene sulfide, CN 85102664); most of the about 2/3 patents relate to the PPS subsequent modification processing category. And few reports are published on the industrial separation, purification and application of the diphenyl sulfide oligomer generated in the polymerization reaction. Through research and development of the p-phenylene sulfide oligomer, a byproduct (the main component of the phenylene sulfide oligomer) generated in the PPS industrialization not only has excellent performances of heat resistance, chemical corrosion resistance and the like, but also can be widely used as a high-end anticorrosive coating in industries of ships, spaceflight and the like as a production raw material for producing other types of special resins through secondary polymerization and modification due to the characteristics of small particle size, easiness in dispersion, easiness in forming and the like.

Currently, the demand for oligomers of diphenyl sulfide is about 15 million tons or more in the market, and is kept at a high rate of 15% per year. However, the domestic industrial yield is only about 2 ten thousand tons, and the supply and demand are seriously deviated, so that the optimization of the production process and the recycling and reasonable utilization of resources such as oligomers, waste residues and the like are key technologies for improving the enterprise competitiveness and reducing the production cost no matter in production enterprises or enterprises to be built.

At present, most of domestic industrial production enterprises continue to use a production process for synthesizing polyphenylene sulfide by compression polymerization in a sodium sulfide method, and the technical problems of product separation, purification and solvent recovery are more: 1) the process flow is long, the equipment manufacturing requirement is high (most of the equipment is made of 304 stainless steel materials), the energy consumption is high, the production period is long, and the final product cost is high; 2) the production operation is difficult to realize continuous and stable production, basically in an intermittent uncontrollable state, and the equipment is easy to damage and has short overhaul period; 3) the waste products in the production process are not effectively separated and purified, so that the oligomer is not fully recovered, and is mixed with waste salt in industrial production, thereby solving the problem of environmental pollution caused by difficult environmental treatment.

The main process flow for industrially generating PPS in China is as follows:

1. the production principle is as follows: using sodium sulfide (Na)₂S) and p-dichlorobenzene (p-DCB) are subjected to polycondensation in an organic aprotic polar solvent such as N-methylpyrrolidone (NMP) at 180-270 ℃ in the presence of a reaction auxiliary agent. The chemical reaction formula is as follows:

2. the main material treatment process flow is shown with reference to fig. 2.

After the reaction product obtained by the polycondensation pressurization method is separated and filtered by a centrifugal machine, the low molecular weight polymer generated in the polymerization reaction is mixed in the resin and the reaction slurry, a small part of the low molecular weight polymer is adhered in the resin, and the influence can be eliminated by a product purification process; however, most of the flocs are retained in the slurry of the synthetic material, and the flocs are mixed to form a solid state, a liquid state and a floc state.

The process is characterized in that the polymerization production operation is basically normal, but the solvent recovery process flow is not smooth, the synthesis slurry is also separated in the early stage, but the components in the product synthesis slurry are complex, the process belongs to a multi-component mixed system, wherein the product synthesis slurry mainly comprises PPS resin fine powder with higher molecular weight, solvent NMP, auxiliary agent lithium chloride, by-product (NaCl), oligomer (diphenyl sulfide oligomer), water, unreacted monomer (p-dichlorobenzene is abbreviated as p-DCB), sodium sulfide, sodium hydroxide, N-containing heterocyclic compound and the like, the materials are not treated in a targeted manner, particularly the low polymer and the N-containing heterocyclic compound contained in the material enter a solvent recovery system and are enriched in pipelines and equipment, the polymer cannot be eradicated from the system effectively, after long-time operation accumulation, industrial production equipment is failed, the production operation is hindered, and the by-product sodium chloride and the auxiliary agent are mixed in the production process, the formed waste slag is difficult to treat and has high treatment cost, thereby causing serious environmental pollution.

Disclosure of Invention

The invention aims to provide a method for recovering a phenylene sulfide oligomer in polyphenylene sulfide production, which is a novel method for effectively recovering the phenylene sulfide oligomer from synthetic material slurry based on the level of the current domestic special engineering Plastic Polyphenylene Sulfide (PPS) industrial production device.

In order to achieve the purpose of the invention, the technical scheme adopted by the invention is as follows:

the invention provides a method for recovering a phenylene sulfide oligomer in polyphenylene sulfide production, which comprises the following steps:

(1) carrying out solid-liquid separation on the synthetic material slurry after the polymerization reaction, washing and drying a filter cake obtained by separation to obtain PPS, and recovering mixed water generated by recovering the PPS into a mixed water storage tank for later use; adding the separated filtrate into an evaporator for reduced pressure evaporation, and adding the residual filtrate into an oligomer extraction tank for later use;

(2) adding the mixed water obtained in the step (1) into an oligomer extraction tank, stirring the mixed water and the residual filtrate to obtain a mixed solution, and then conveying the mixed solution to a first-stage plate-and-frame filter for filtering;

(3) recycling the filter cake collected after the filtration of the first-stage plate and frame filter in the step (2) into a fine powder storage tank, mixing the filter cake with the PPS in the step (1) to obtain a mixture, adding hot water, stirring uniformly, conveying the mixture to the first-stage plate and frame filter for secondary filtration, drying the filter cake collected after the filtration, recycling, and conveying the filtrate obtained after the first filtration of the first-stage plate and frame filter to the second-stage plate and frame filter for filtration;

(4) recovering the filter cake collected after the filtration by the second-stage plate-and-frame filter in the step (3) into a low polymer storage tank, adding hot water, uniformly stirring, conveying to the second-stage plate-and-frame filter, filtering again to obtain a semi-finished product of the diphenyl sulfide oligomer, and drying the filter cake in vacuum to obtain the diphenyl sulfide oligomer; and (4) carrying out the next salt recovery process on the filtrate obtained after the first filtration of the second-stage plate-and-frame filter.

Preferably, in the step (1), the temperature of the synthetic material slurry is 70-90 ℃.

Preferably, in the step (1), the filter cake obtained by separation is washed, purified, prepared into slurry, centrifugally separated and dried to obtain PPS, and the mixed water of the washing water and the slurry preparation water generated in the washing and slurry preparation processes is recycled into a mixed water storage tank for later use.

Preferably, in the step (1), the adding amount of the filtrate is 60-70% of the volume of the evaporator, the vacuum degree of the evaporator is-0.05-0.08 MPa, the temperature is 90-140 ℃, and the rotating speed is 80-120 rmp/min.

Preferably, in the step (1), after the filtrate is evaporated under reduced pressure, the volume of the remaining filtrate is 20 to 25% of the volume of the filtrate before evaporation, and when the mass of the solvent NMP remaining in the remaining filtrate is 20 to 30%, the evaporation under reduced pressure of the filtrate is stopped.

Preferably, in the step (1), the solvent NMP is recovered after condensing a gas phase obtained by evaporating the filtrate under reduced pressure.

Preferably, in the step (2), the rotation speed of the oligomer extraction tank is 40-60 rpm/min, the temperature is 60-80 ℃, and the stirring time is 10-15 min.

Preferably, in the step (2), the mass ratio of the mixed water to the residual solvent NMP in the remaining filtrate is 8 to 10: 1.

Preferably, in the step (3), the temperature of the hot water is 50-60 ℃, and the mass ratio of the mixture to the hot water is 1: 2-3.

Preferably, in the step (4), the vacuum degree of the vacuum drying is-0.05 to-0.08 Mpa, and the temperature is 80 to 90 ℃.

The invention has the following beneficial effects:

1. the invention successfully recovers a new product of the diphenyl sulfide oligomer by optimizing and improving the process conditions of the synthetic material slurry, meets the production requirements of high-grade paint and modified filler by methods such as modification and the like due to the excellent performances of heat resistance, chemical corrosion resistance and the like similar to PPS resin and also due to the characteristics of small particle diameter, easy dispersion, easy forming and the like, and promotes the application of the diphenyl sulfide oligomer as the paint in the military industry and the ship industry.

2. NMP recovered by the evaporator can directly return to a polymerization process to meet the requirement of reproduction, rectification and recovery are not needed, and the production period is shortened while energy is saved; in the invention, the water for separating out and separating the oligomer comes from the intermediate materials in the system, thus realizing the comprehensive cyclic utilization of water resources;

3. according to the invention, a filtrate diversified system is effectively separated through an oligomer recovery process, oligomers are separated from the system, N-type heterocyclic substances and benzene series polymers still remain in residual NMP, and inorganic salts are completely dissolved in a water system, so that necessary conditions are provided for the next salt recovery process, and the method has important environmental protection significance for reducing the amount of waste residues and waste water and treating.

4. The method effectively recovers oligomers, ensures the continuity and stability of production, shortens the production period, ensures the operation efficiency of equipment, saves energy, reduces consumption, reasonably recycles resources, greatly reduces the production cost and improves the market competitiveness of products.

Drawings

FIG. 1 is a process flow diagram of the present invention;

FIG. 2 is a process flow diagram of the prior art.

Detailed Description

The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

Unless otherwise indicated, the technical means used in the examples are conventional means well known to those skilled in the art.

Referring to fig. 1, the method for recovering the phenylene sulfide oligomer in the invention is suitable for the production process of synthesizing the polyphenylene sulfide by the sodium sulfide method through compression polymerization.

According to the invention, through researching the characteristics of the main component of the diphenyl sulfide oligomer of the oligomer, the diphenyl sulfide oligomer can be completely dissolved in NMP at the temperature of more than 180 ℃, but is insoluble in water, and is separated out from the NMP in the presence of water to form floccule, and meanwhile, the polyphenylene sulfide oligomer has the characteristics of thermoplastic resin similar to PPS resin, and specific differences are shown in the following table 1. In the table, the crystallization temperature is related to the process control.

TABLE 1 comparison table of technical indexes of phenylene sulfide oligomer and PPS resin

The invention provides a method for recovering a phenylene sulfide oligomer in polyphenylene sulfide production, which specifically comprises the following steps:

step (1): directly sending the synthetic material slurry after the polymerization reaction to a high-speed centrifuge for solid-liquid separation; washing, purifying, preparing slurry, centrifugally separating and drying the separated filter cake to obtain PPS, and recycling washing water and slurry preparation water generated in the washing and slurry preparation processes into a mixed water storage tank for later use; and adding the separated filtrate into an evaporator for reduced pressure evaporation, condensing a gas phase by a condenser, recovering to obtain a solvent NMP, and adding the residual filtrate after reduced pressure evaporation into an oligomer extraction tank for later use.

Specifically, ① controls the temperature of the synthetic material slurry to 70-90 ℃, prevents a small amount of water in the synthetic material slurry from gasifying at an over-high temperature and simultaneously takes away part of NMP to cause loss of the NMP and environmental pollution, and prevents oligomers in the synthetic material slurry from being partially precipitated and naturally settled to be adsorbed in pores inside the semi-finished product PPS resin to cause quality reduction of the finished product.

The centrifugal machine adopts a stainless steel screen, the mesh number is 200-250 meshes, a large amount of semi-finished PPS resin can be recovered, the fine PPS powder amount in subsequent procedures is reduced, and the recovery rate of products is improved.

The resulting wash water and slurrying water are used as extractants for the extraction of oligomeric compounds.

② adding the separated filtrate into an evaporator with stirring function, and performing reduced pressure evaporation, wherein the volume of the added filtrate is 60-70% of the volume of the evaporator, the gas and liquid phases have a certain separation space during heating separation, the vacuum degree is-0.05-0.08 MPa, the temperature is 90-140 ℃, and the rotation speed is 80-120 rmp/min.

The reduced pressure evaporation of the invention is carried out in two steps: firstly, evaporating distillate at 90-110 ℃ to be directly used as a mixed solvent for extracting oligomer, wherein the distillate comprises 2-5% of solvent NMP and 95-98% of water; and secondly, directly collecting evaporated distillate into a solvent recovery tank at 110-140 ℃, wherein the distillate comprises 99% of solvent NMP and 1% of water, and the solvent NMP can be added into a rectification system for purification, and the recovered solvent NMP can be directly used in the production of PPS resin. The temperature should not be too high, which would cause oxidation and degradation of the oligomer attached to the inner wall of the evaporator. It should be noted that: the evaporation distillate is a liquid which flows out after a gas phase obtained by carrying out reduced pressure evaporation on the separated filtrate is condensed.

In the process of carrying out reduced pressure evaporation on the filtrate, when the residual amount of the filtrate in the evaporator is 20-25% of the volume of the filtrate before evaporation and the mass of a solvent NMP (N-methyl pyrrolidone) remained in the residual filtrate is detected to be 20-30%, closing the evaporator, filling nitrogen and returning pressure (returning to normal pressure), and adding the residual filtrate and washing water for washing the inner wall of the evaporator into a low polymer extraction tank with a stirring function to extract low polymers. The residual solvent NMP had the N-containing heterocyclic compound dissolved therein, and all the inorganic salt impurities were transferred and dissolved in water.

By adopting reduced pressure evaporation, the oligomer can be prevented from being oxidized and degraded when being contacted with air, and the subsequent recovery is not facilitated.

Step (2): adding the mixed water of the washing water and the pulping water in the mixed water storage tank in the step (1) into an oligomer extraction tank, stirring the mixed water and the residual filtrate to obtain a mixed solution, controlling the rotating speed to be 40-60 rpm/min, fully stirring the mixed solution at the temperature of 60-80 ℃ for 10-15 min, and pumping the mixed solution into a first-stage plate-and-frame filter by a slurry pump for filtering; wherein the adding amount of the mixed water is 8-10: 1 according to the mass ratio of the mixed water to the residual solvent NMP in the residual filtrate.

Step (3), recycling the filter cake collected after the filtration of the first-stage plate-and-frame filter in the step (2) into a fine powder storage tank, mixing the filter cake with the PPS collected in the step (1) to obtain a mixture, adding hot water, uniformly stirring, conveying the mixture to the first-stage plate-and-frame filter through a slurry pump for secondary filtration to obtain a filter cake which is semi-finished product PPS fine powder, washing the semi-finished product PPS fine powder for multiple times, recycling the generated washing water and the filtrate after the secondary filtration into a mixed water storage tank to be used as an extractant of low polymers, directly feeding the washed filter cake into a finished product PPS drying process, and recycling the PPS fine powder; the filtrate obtained by the first filtration of the first-stage plate and frame filter is directly conveyed to the second-stage plate and frame filter for filtration; wherein the temperature of the hot water is 50-60 ℃, and the mass ratio of the mixture to the hot water is 1: 2-3; the pore of the filter cloth in the first-stage plate-and-frame filter is 50-100 mu m.

Step (4), recovering the filter cake collected after the filtration by the second-stage plate-and-frame filter in the step (3) into a low polymer storage tank, adding hot water, uniformly stirring, conveying to the second-stage plate-and-frame filter through a slurry pump, carrying out secondary filtration to obtain a semi-finished product of the diphenyl sulfide oligomer, washing the filter cake for multiple times, recovering the obtained washing water and the filtrate after the secondary filtration into a mixed water storage tank to be used as an extractant of the oligomer, and carrying out vacuum drying on the filter cake collected after washing to obtain the diphenyl sulfide oligomer; and collecting the filtrate obtained by the first filtration of the second-stage plate and frame filter into a sodium chloride mixed liquid tank, and carrying out the next salt recovery process, wherein the salt recovery process is the prior art. Wherein, the pores of the filter cloth in the second-stage plate-and-frame filter are 1-5 μm, and the filter cloth can be replaced by the first-stage plate-and-frame filter; the vacuum degree of vacuum drying is-0.05 to-0.08 Mpa, and the temperature is 80 to 90 ℃.