CN215288581U - Complete equipment for producing cationic polymer monomer by continuous reaction - Google Patents

Complete equipment for producing cationic polymer monomer by continuous reaction Download PDF

Info

Publication number
CN215288581U
CN215288581U CN202120582428.7U CN202120582428U CN215288581U CN 215288581 U CN215288581 U CN 215288581U CN 202120582428 U CN202120582428 U CN 202120582428U CN 215288581 U CN215288581 U CN 215288581U
Authority
CN
China
Prior art keywords
reactor
pipeline
normal pressure
cation
communicated
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN202120582428.7U
Other languages
Chinese (zh)
Inventor
荣帅
王兵杰
燕翔
于翔
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shandong Lanwan New Material Co ltd
Original Assignee
Shandong Lanwan New Material Co ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Shandong Lanwan New Material Co ltd filed Critical Shandong Lanwan New Material Co ltd
Priority to CN202120582428.7U priority Critical patent/CN215288581U/en
Application granted granted Critical
Publication of CN215288581U publication Critical patent/CN215288581U/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Landscapes

  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The utility model relates to the field of chemical production, in particular to a complete set of device for producing cationic polymer monomers by continuous reaction, which comprises a main reaction area, a stripping tower, an atmospheric reaction area, a tail gas washing area and a product cooling area, wherein the main reaction area is communicated with the stripping tower, the bottom of the stripping tower is communicated with the atmospheric reaction area, one end of the atmospheric reaction area is communicated with the tail gas washing area and treats and recovers tail gas, and the other end of the atmospheric reaction area is communicated with the product cooling area and produces finished products; the utility model discloses polymerization inhibitor lectotype and quantity are reasonable, and continuous production ability is strong, and the automated control level is high, and production efficiency is high, product quality is stable.

Description

Complete equipment for producing cationic polymer monomer by continuous reaction
Technical Field
The utility model relates to the field of chemical equipment, concretely relates to complete equipment for producing cationic polymer monomers by continuous reaction.
Background
The cationic polymer is a water-soluble polymer with the largest dosage and the widest application range at present, and has high application value in the fields of petrochemical industry, papermaking, textile printing and dyeing, daily chemicals, particularly as a flocculating agent in water treatment, sludge dewatering and the like. Cationic monomers are the base stock for cationic polymers. Cationic monomers are various, and mainly comprise quaternary ammonium salt, quaternary phosphonium salt, quaternary sulfonium salt cationic monomers and the like, wherein the mechanical force survivability of DAC cationic polymers for forming floccules is far better than that of DMC flocculants, and the cationic monomers are polymer flocculant products which are most widely applied and used at present. Because the integrated equipment that realizes DAC cation monomer industrial production is less in China, there are polymerization inhibitor selection type and quantity improper, the automation control level is low to the contrast patent device, it is poor to produce the ability in succession, low in production efficiency, product quality unstability scheduling problem, high-quality DAC class cation polymer still has certain breach in the domestic market, consequently, the market is urgent to wait to promote a continuous reaction production cation polymer monomer integrated equipment to enlarge DAC class monomer productivity, satisfy domestic high-quality DAC class flocculating agent product demand.
The patent with the application number of CN201721650499.6 discloses a cation polyacrylamide production line, which comprises a dissolving tank, a waste gas washer, a delivery pump, a reactor, an air compressor, an auger, a granulator, a dryer, a cyclone dust collector, a draught fan, a sieving machine, a grinding machine, a packing machine and a bag-type dust collector, wherein the dissolving tank is connected with the reactor through a delivery pump material, the dissolving tank and the reactor are respectively connected with two waste gas washers, the upper part of the reactor is connected with the air compressor, the lower part of the reactor is connected with the granulator through the auger, the granulator is connected with the dryer, the lower part of the dryer is connected with a hot air pipeline, the upper part of the dryer is provided with the cyclone dust collector, one side of the dryer is connected with the draught fan and connected with the sieving machine, the grinding machine is arranged below the sieving machine, the grinding machine is connected with the granulating machine, the bag-type dust collector is connected above the sieving machine, the sieving machine is connected with the packing machine, and the device is not provided with a multi-stage processing structure and a multi-cooling structure, the treatment is insufficient, and when the flow is too large, the treatment cannot be carried out, so that accidents such as blockage and the like occur, the continuous production capacity is poor, the production efficiency is low, and the product quality is unstable.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the not enough of above-mentioned current device, develop a polymerization inhibitor lectotype and quantity reasonable, automated control level is high, and continuous production ability is strong, the cationic polymer monomer DAC's integrated equipment that production efficiency is high, product quality is stable.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a complete set of equipment for producing cationic polymer monomers by continuous reaction comprises a main reaction zone, a stripping tower, an atmospheric pressure reaction zone, a tail gas washing zone, a product cooling zone, a compressed air pipeline, a deionization process water pipeline, a dimethylamine ethyl acrylate pipeline and a methane chloride pipeline, wherein the deionization process water pipeline, the dimethylamine ethyl acrylate pipeline and the methane chloride pipeline are communicated with the main reaction zone and inject production raw materials into the main reaction zone; the compressed air pipeline is respectively communicated with the main reaction zone and the normal pressure reaction zone and injects excessive compressed air into the main reaction zone and the normal pressure reaction zone, and the deionization process water pipeline is also provided with branches and is communicated with the top of the stripping tower and injects deionization process water into the top of the stripping tower.
Preferably, the main reaction zone comprises a main cation reactor, an auxiliary cation reactor A, an auxiliary cation reactor B and a material transfer pump; the deionization process water pipeline, the dimethylamine ethyl acrylate pipeline and the methane chloride pipeline are communicated with the top of the main cation reactor and inject production raw materials into the main cation reactor, the bottom of the main cation reactor is provided with a pipeline and is connected with the material transfer pump, and a pipeline on one side of the material transfer pump is communicated with the main cation reactor to form a secondary treatment structure; the pipeline on the other side of the material transferring pump is communicated with the secondary cation reactor A to form a secondary treatment structure; the bottom of the auxiliary cation reactor A is provided with a pipeline and is communicated with the auxiliary cation reactor B to form a three-stage treatment structure; the top of the main cation reactor, the top of the auxiliary cation reactor A and the top of the auxiliary cation reactor B are all provided with gas phase pipelines and communicated with the upper part of the stripping tower, and the bottom of the auxiliary cation reactor B is provided with a pipeline and communicated with the middle part of the stripping tower.
Preferably, the bottom of the stripping tower is provided with a pipeline and is connected with the normal-pressure reaction zone, and the top of the stripping tower is provided with a gas phase pipeline and is communicated with the tail gas washing zone; the normal pressure reaction zone comprises a normal pressure reactor A and a normal pressure reactor B; the normal pressure reactor A is provided with an overflow pipeline and is communicated with the normal pressure reactor B; and the bottoms of the normal pressure reactor A and the normal pressure reactor B are both provided with pipelines and are connected with a product cooling area.
Preferably, the product cooling zone comprises a product pump and a product cooler, and one end of the product pump is communicated with the normal pressure reactor A and the normal pressure reactor B; the other end of the product pump is connected with the product cooler, and the product pump is also provided with a side outlet pipeline and is communicated with the normal pressure reactor B; the tail gas washing district includes tail gas washing tower, spray circulating pump and cooler, thereby tail gas washing tower passes through spray circulating pump with the cooler is connected and is formed tail gas spray cooling circulation closed circuit and handle the recovery tail gas, the strip tower top be provided with the pipeline and with tail gas washing tower intercommunication.
Preferably, the top of the normal pressure reactor A, the top of the normal pressure reactor B and the top of the tail gas washing tower are provided with tail gas recovery pipelines, and the outlets of the tail gas recovery pipelines are provided with tail gas recovery systems.
Preferably, the top parts of the main cation reactor, the auxiliary cation reactor A, the auxiliary cation reactor B, the normal pressure reactor A and the normal pressure reactor B are all provided with accident unloading lines, and the tail ends of the accident unloading lines are provided with accident tanks.
Preferably, cooling coils are arranged inside the main cation reactor, the auxiliary cation reactor A, the auxiliary cation reactor B, the normal pressure reactor A and the normal pressure reactor B, a circulating cooling pump and an external circulating cooler are further arranged outside the main cation reactor, and the main cation reactor, the circulating cooling pump and the external circulating cooler form a cooling circulation closed loop structure of the main cation reactor.
Preferably, main cation reactor, vice cation reactor, ordinary pressure reactor and ordinary pressure reactor all are provided with control system and automatic control valve, the top of main cation reactor is provided with the counter, deionization process water pipeline, dimethylamine ethyl acrylate pipeline and methane chloride pipeline with the counter intercommunication forms the feeding control structure.
Compared with the prior art, the utility model, have following advantage:
1. the utility model adopts the way of filling the excessive air into the reaction area to achieve the purpose of inhibiting polymerization, thereby reducing the consumption of polymerization inhibitor, being beneficial to improving the product purity and reducing the steam stripping separation investment of the subsequent flow;
2. the continuous reaction of a plurality of reactors and the sequential feeding and discharging design are adopted, so that the production continuity is maintained conveniently;
3. the reactor adopts a cooling design combining internal circulation cooling and reaction material backflow, so that the cooling effect is improved, the reaction temperature fluctuation is reduced, and the reaction yield is improved;
4. the stripping tower adopts an ion water spraying system, a gas phase and liquid phase branch inlet path and an anti-polymerization filler design, and the gas phase and liquid phase dynamics principle is fully utilized, so that the gas phase separation efficiency and the product purity are improved;
5. the control and detection equipment of the device adopts automation equipment, so that the remote centralized control, management and operation of the real device are realized, the labor intensity of workers is greatly reduced, and the overall production efficiency is improved.
Drawings
Fig. 1 is a schematic structural view of the present invention;
in the figure: 1-main cation reactor, 2-auxiliary cation reactor A, 3-auxiliary cation reactor B, 4-stripping tower, 5-normal pressure reactor A, 6-normal pressure reactor B, 7-tail gas washing tower, 8-external circulating cooler, 9-product cooler, 10-cooler, 11-circulating cooling pump, 12-material transfer pump, 13-product pump, 14-spraying circulating pump, 15-accident unloading line, 16-accident tank, 17-compressed air line, 18-deionization process water line, 19-dimethylamine ethyl acrylate line, 20-methyl chloride line, 21-tail gas recovery line, 22-gas phase line, 23-meter, 24-tail gas recovery system, 25-liquid phase line.
Detailed Description
In the following description, numerous implementation details are set forth in order to provide a more thorough understanding of the present invention. It should be understood, however, that these implementation details should not be used to limit the invention. That is, in some embodiments of the invention, details of these implementations are not necessary. In addition, some conventional structures and components are shown in simplified schematic form in the drawings.
Example one
Referring to FIG. 1, an embodiment of a continuous reaction plant for producing cationic polymer monomers is shown below: deionized process water, dimethylamine ethyl acrylate and methane chloride respectively enter the main cation reactor 1 from the corresponding deionized process water pipeline 18, dimethylamine ethyl acrylate pipeline 19 and methane chloride pipeline 20 through the meter 23, the three pipelines are respectively connected with the meter 23, and the accurate proportioning of reactants can be ensured by the accurate control of the meter 23, thereby avoiding the waste of raw materials.
The main cation reactor 1 and the circulation cooler 8 form a cooling circulation closed loop structure through a circulation cooling pump 11. The arrangement of the cooling circulation closed-loop structure can improve the cooling effect, build proper reaction temperature and reduce the fluctuation of the reaction temperature.
The discharge pipe at the bottom of the main cation reactor 1 is connected with the material transfer pump 12, the outlet pipe of the material transfer pump 12 is connected with the main cation reactor 1 and the feeding pipe at the top of the auxiliary cation reactor A2, the material transfer pump 12 is used as a flow direction controller at the moment, if the reactant does not meet the design requirement, the switch of the main cation reactor 1 is opened, the reactant flows back into the main cation reactor 1 to continue to react, if the reactant reaches the design criterion, the switch of the negative cation reactor A2 is opened, and the reactant enters the negative cation reactor A2 to carry out the next reaction.
The discharge pipeline at the bottom of the secondary cationic reactor A2 is connected with the feed pipeline at the top of the secondary cationic reactor B3, the main cationic reactor 1, the secondary cationic reactor A2 and the secondary cationic reactor B3 are in a step reaction progress, the reactant in the last stage can flow into the next stage to continue the reaction when reaching the design requirement, and the multi-stage reaction can ensure the full reaction of the substance on the one hand and the full cooling of the substance on the other hand.
The main cation reactor 1, the secondary cation reactor A2 and the secondary cation reactor B3 are connected with a feeding pipeline at the upper part of the stripping tower 4 through a top gas phase pipeline 22, a liquid phase pipeline 25 at the bottom part of the secondary cation reactor B3 is connected with a feeding pipeline at the lower part of the stripping tower 4, and the gas phase and liquid phase dynamics principles are fully utilized by the separation design of the gas phase pipeline 22 and the liquid phase pipeline 25, so that the gas phase separation efficiency and the product purity are improved.
Stripping tower 4 adopts ion water spraying system and prevents the design of polymerization filler, 4 bottom discharge line of stripping tower and ordinary pressure reactor A5 top charge-in line connection, the spraying system at stripping tower 4 top is connected with deionization process water pipeline 18, 4 top gas phase line of stripping tower and tail gas scrubbing tower 7 charge-in line connection, through the reuse to deionization process water, can be abundant with the separation and purification of reactant, the tail gas after the purification passes through tail gas recovery pipeline 21 and gets into tail gas recovery system 24 and can also retrieve the material that does not react completely when having avoided the pollution to the environment.
The normal pressure reactor A5 is connected with the normal pressure reactor B6 through a side overflow line, the normal pressure reactor A5 is connected with a product pump 13 feeding line through a discharging line at the bottom of the normal pressure reactor B6, the main cation reactor 1, the auxiliary cation reactor A2, the auxiliary cation reactor B3, the normal pressure reactor A5 and the normal pressure reactor B6 adopt timing reaction, and the design of feeding and discharging materials in sequence can ensure the continuity of production and improve the reaction efficiency at the same time.
The tops of the main cation reactor 1, the auxiliary cation reactor A2, the auxiliary cation reactor B3, the normal pressure reactor A5 and the normal pressure reactor B6 are all provided with compressed air pipelines 17, and a certain amount of excess air is introduced to prevent the polymerization of reactants, so that the use amount of a polymerization inhibitor is reduced, the product purity is improved, and the stripping separation investment of the subsequent flow is reduced; the main cation reactor 1, the auxiliary cation reactor A2, the auxiliary cation reactor B3, the normal pressure reactor A5 and the normal pressure reactor B6 are internally provided with cooling coils, wherein in order to ensure the cooling effect, the main cation reactor 1 is also provided with an external circulating cooler 8, the reaction substances can be ensured to be fully cooled through the combination of internal cooling and external cooling, the temperature fluctuation of the reaction substances is reduced, and the reaction efficiency is improved.
A main discharge pipeline of the product pump 13 is connected with the product cooler 9, and the produced product is cooled by the product cooler 9 and then enters a product tank area; the tail gas washing tower 7 and the cooler 10 form a tail gas spraying and cooling circulation closed circuit through a spraying and circulating pump 14, the tail gas is further treated, and the washed tail gas is separated by a tail gas recovery system and then is reused; the washing residual liquid after precipitation is treated by a sewage treatment system and then is discharged after reaching the standard, so that the pollution to the environment is reduced; the main cation reactor 1, the auxiliary cation reactor A2, the auxiliary cation reactor B3, the normal pressure reactor A5 and the normal pressure reactor B6 are all provided with an accident discharging line 15 and an accident tank 16, so that a buffer discharging area exists when an accident occurs, and the safety of the device is enhanced.
The main production equipment of the device is provided with a distributed control system and a programmable controller, the feeding and discharging pipelines are provided with automatic control valves, and the pressure gauge, the flowmeter, the thermometer and the like of the equipment are automatic equipment.
The process flow is as follows:
deionized process water, dimethyl amine ethyl acrylate and methane chloride raw material pipelines pass through a metering pump and are fed from the top of a main cation reactor 1 according to a designed flow, the reaction is an exothermic reaction, the main cation reactor 1 and a circulating cooler 8 form a cooling circulation closed loop through a circulating cooling pump 11, the pressure is maintained between 0.95 and 0.75MPa, the temperature is maintained between 35 and 50 ℃, the reaction time is maintained between 0.8 and 1.5 hours, and if the reactants do not meet the design requirements, the reactants can be refluxed and then reacted; after the reactants meet the requirements, pumping the reactants into a secondary cation reactor A2 through a discharge pipeline at the bottom of a main cation reactor 1 and a material transfer pump 12 to continue the reaction, wherein the reaction conditions refer to the main cation reactor 1, and the pressure can be reduced by about 0.3MPa according to the reaction conditions; after the designed reaction time is reached, the reactants are pressed into a secondary cationic reactor B3 by means of compressed air power, the reaction time and the pressure reference of a secondary cationic reactor B3 and the temperature of a secondary cationic reactor A2 are carried out according to the natural temperature, and the designed excess air is used in the three reactors to prevent the product from polymerizing and improve the product yield.
The method comprises the following steps that a main cation reactor 1, an auxiliary cation reactor A2 and an auxiliary cation reactor B3 are fed from a feeding pipeline at the upper part of a stripping tower 4 through a top gas phase pipeline, a liquid phase reactant reaching a specified reaction time in an auxiliary cation reactor B3 is fed from a feeding pipeline at the lower part of the stripping tower 4, after spraying and gas stripping, the liquid phase reactant in the stripping tower 4 is pressed into an atmospheric reactor A5 under pressure, the liquid phase reactant in the atmospheric reactor A5 reaches the specified liquid level and then flows into an atmospheric reactor B6 through a side overflow line, the reaction time of the atmospheric reactor is maintained within 0.8h to 1.5h, the two reactors work simultaneously, after the liquid phase reactant reaches the reaction time and is pumped into a product cooler 9 through a product pump 13 for cooling, a cation monomer product is sent to a tank area, the two atmospheric reactors maintain excessive air injection in the reaction process, and a tail gas removal and recovery system is used for tail gas removal.
All reactors of the device are designed with accident discharging lines, and unqualified reaction materials can pass through the accident discharging lines to the accident tank when the device is abnormal or power failure occurs.
The gas phase product of the stripping tower 4 enters a tail gas washing tower 7, the tail gas washing tower 7 and a cooler 10 form a tail gas spraying cooling circulation closed circuit through a spraying circulating pump 14, the washed tail gas is separated by a tail gas recovery system and then is recycled, and the washing residual liquid after precipitation is treated by a decontamination water treatment system and then is discharged after reaching the standard.
The present invention is not limited to the above-described embodiments, and various changes can be made within the knowledge range of those skilled in the art without departing from the spirit of the present invention, and the changed contents still belong to the protection scope of the present invention.

Claims (8)

1. A kit for the continuous reaction production of cationic polymer monomers, characterized by: the device comprises a main reaction zone, a stripping tower, an atmospheric pressure reaction zone, a tail gas washing zone, a product cooling zone, a compressed air pipeline, a deionization process water pipeline, a dimethyl amine ethyl acrylate pipeline and a methane chloride pipeline, wherein the deionization process water pipeline, the dimethyl amine ethyl acrylate pipeline and the methane chloride pipeline are communicated with the main reaction zone and inject production raw materials into the main reaction zone, the main reaction zone is communicated with the stripping tower through a pipeline, the bottom of the stripping tower is communicated with the atmospheric pressure reaction zone through a pipeline, the upper end of the atmospheric pressure reaction zone is communicated with the tail gas washing zone, and the lower end of the atmospheric pressure reaction zone is communicated with the product cooling zone and produces finished products;
the compressed air pipeline is respectively communicated with the main reaction zone and the normal pressure reaction zone and injects excessive compressed air into the main reaction zone and the normal pressure reaction zone, and the deionization process water pipeline is also provided with branches and is communicated with the top of the stripping tower and injects deionization process water into the top of the stripping tower.
2. The plant for the continuous reaction production of cationic polymer monomers according to claim 1, wherein: the main reaction zone comprises a main cation reactor, an auxiliary cation reactor A, an auxiliary cation reactor B and a material transfer pump;
the deionization process water pipeline, the dimethylamine ethyl acrylate pipeline and the methane chloride pipeline are communicated with the top of the main cation reactor and inject production raw materials into the main cation reactor, the bottom of the main cation reactor is provided with a pipeline and is connected with the material transfer pump, and a pipeline on one side of the material transfer pump is communicated with the main cation reactor to form a secondary treatment structure; the pipeline on the other side of the material transferring pump is communicated with the secondary cation reactor A to form a secondary treatment structure; the bottom of the auxiliary cation reactor A is provided with a pipeline and is communicated with the auxiliary cation reactor B to form a three-stage treatment structure;
the top of the main cation reactor, the top of the auxiliary cation reactor A and the top of the auxiliary cation reactor B are all provided with gas phase pipelines and communicated with the upper part of the stripping tower, and the bottom of the auxiliary cation reactor B is provided with a liquid phase pipeline and communicated with the middle part of the stripping tower.
3. The plant for the continuous reaction production of cationic polymer monomers according to claim 2, wherein: the bottom of the stripping tower is provided with a pipeline and is connected with the normal pressure reaction zone, and the top of the stripping tower is provided with a gas phase pipeline and is communicated with the tail gas washing zone;
the normal pressure reaction zone comprises a normal pressure reactor A and a normal pressure reactor B; the normal pressure reactor A is provided with an overflow pipeline and is communicated with the normal pressure reactor B; and the bottoms of the normal pressure reactor A and the normal pressure reactor B are both provided with pipelines and are connected with a product cooling area.
4. The plant for the continuous reaction production of cationic polymer monomers according to claim 3, wherein: the product cooling zone comprises a product pump and a product cooler, and one end of the product pump is communicated with the normal pressure reactor A and the normal pressure reactor B; the other end of the product pump is connected with the product cooler, and the product pump is also provided with a side outlet pipeline and is communicated with the normal pressure reactor B;
the tail gas washing district includes tail gas washing tower, spray circulating pump and cooler, thereby tail gas washing tower passes through spray circulating pump with the cooler is connected and is formed tail gas spray cooling circulation closed circuit and handle the recovery tail gas, the strip tower top be provided with the pipeline and with tail gas washing tower intercommunication.
5. The plant for the continuous production of cationic polymer monomers according to claim 3 or 4, wherein: and tail gas recovery pipelines are arranged at the tops of the normal pressure reactor A, the normal pressure reactor B and the tail gas washing tower, and a tail gas recovery system is arranged at an outlet of each tail gas recovery pipeline.
6. The plant for the continuous reaction production of cationic polymer monomers according to claim 3, wherein: accident unloading lines are arranged at the tops of the main cation reactor, the auxiliary cation reactor A, the auxiliary cation reactor B, the normal pressure reactor A and the normal pressure reactor B, and an accident tank is arranged at the tail end of the accident unloading line.
7. The plant for the continuous reaction production of cationic polymer monomers according to claim 3, wherein: the main cation reactor, the auxiliary cation reactor A, the auxiliary cation reactor B, the normal pressure reactor A and the normal pressure reactor B are internally provided with cooling coils, the outside of the main cation reactor is also provided with a circulating cooling pump and an external circulating cooler, and the main cation reactor, the circulating cooling pump and the external circulating cooler form a cooling circulation closed loop structure of the main cation reactor.
8. The plant for the continuous production of cationic polymer monomers according to claim 3 or 4, wherein: the device comprises a main cation reactor, a secondary cation reactor A, a secondary cation reactor B, a normal pressure reactor A and a normal pressure reactor B, wherein the main cation reactor, the secondary cation reactor A, the secondary cation reactor B, the normal pressure reactor A and the normal pressure reactor B are respectively provided with a control system and an automatic control valve, the top of the main cation reactor is provided with a meter, and a deionization process water pipeline, a dimethyl amine ethyl acrylate pipeline and a methane chloride pipeline are communicated with the meter to form a feeding control structure.
CN202120582428.7U 2021-03-23 2021-03-23 Complete equipment for producing cationic polymer monomer by continuous reaction Active CN215288581U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202120582428.7U CN215288581U (en) 2021-03-23 2021-03-23 Complete equipment for producing cationic polymer monomer by continuous reaction

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202120582428.7U CN215288581U (en) 2021-03-23 2021-03-23 Complete equipment for producing cationic polymer monomer by continuous reaction

Publications (1)

Publication Number Publication Date
CN215288581U true CN215288581U (en) 2021-12-24

Family

ID=79534150

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202120582428.7U Active CN215288581U (en) 2021-03-23 2021-03-23 Complete equipment for producing cationic polymer monomer by continuous reaction

Country Status (1)

Country Link
CN (1) CN215288581U (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114773214A (en) * 2022-03-30 2022-07-22 山东蓝湾新材料有限公司 Industrial preparation method of acryloyloxyethyl trimethyl ammonium chloride

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114773214A (en) * 2022-03-30 2022-07-22 山东蓝湾新材料有限公司 Industrial preparation method of acryloyloxyethyl trimethyl ammonium chloride
CN114773214B (en) * 2022-03-30 2023-11-17 山东蓝湾新材料有限公司 Industrial preparation method of acryloyloxyethyl trimethyl ammonium chloride

Similar Documents

Publication Publication Date Title
CN106282560B (en) The extraction and cleaning control technique of nickel in acid solution containing nickel
CN110054164B (en) Concentrated recovery system of dilute sulfuric acid
CN215288581U (en) Complete equipment for producing cationic polymer monomer by continuous reaction
CN103933923A (en) Continuous reaction production line consisting of multiple serially connected reaction kettles
CN212655517U (en) Dual-mode switching operation metallurgical wastewater softening device
CN104496758A (en) M-cresol and p-cresol alkylated continuous reaction method
CN109000217B (en) Full-circulation system and method for feeding water and adding ammonia of power plant boiler
CN101935080B (en) High-concentration ammonia nitrogen blowoff treatment system
CN111233231A (en) Complete ammonium phosphate condensate treatment device and treatment and recycling method
CN110563110A (en) Production process of polyaluminum chloride
CN217732690U (en) Retrieve gaseous device of different concentration SO2 in follow waste liquid
CN202542834U (en) Polycrystalline silicon waste acid reclaiming device and polyaluminium chloride (PAC) production device using same
CN212431916U (en) Acid washing device of circulating gas heat exchanger
CN104696946A (en) Process and process system for steam exhaust liquid heat energy recovery and desalted water recovery
CN214973960U (en) Production device for preparing high-molecular polymer intermediate through esterification reaction
CN202754930U (en) High-capacity polyamide slicing polymerization system with multiple-effect evaporation function
CN211936939U (en) Energy-saving environment-friendly external circulation spraying system for polyether production
CN204841602U (en) Device is added to catalyst in petroleum resin production technology
CN102416297A (en) Technical method for recovering waste alkali liquor with composite ceramic membrane in washing of beer bottles
CN203558989U (en) Extraction system for polyoxymethylene dimethyl ether preparation device
CN113230833A (en) Novel ammonia absorption and crystallized salt separation method
CN113413858A (en) High molecular polymer intermediate production device and process flow
CN104177235B (en) A kind of catalyst recycle unit and method preparing polymethoxy dimethyl ether
CN205616822U (en) Yellow water concentration and organic matter recovery unit
CN2835227Y (en) Low-pressure treatment device for waste liquid from synthetic ammonia and urea

Legal Events

Date Code Title Description
GR01 Patent grant
GR01 Patent grant