CN210545133U - In-kettle heat exchange polymerization reaction system for strong exothermic polymerization reaction - Google Patents
In-kettle heat exchange polymerization reaction system for strong exothermic polymerization reaction Download PDFInfo
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- CN210545133U CN210545133U CN201921272629.6U CN201921272629U CN210545133U CN 210545133 U CN210545133 U CN 210545133U CN 201921272629 U CN201921272629 U CN 201921272629U CN 210545133 U CN210545133 U CN 210545133U
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Abstract
The utility model discloses a heat transfer polymerization reaction system in cauldron for strong exothermic polymerization reaction, include: the system comprises a reaction kettle, a polymerized monomer feeding and diluting unit, a power driving unit, a heat exchange unit, a pressure control unit, a catalyst feeding control unit and an initial polymerized monomer or solvent feeding control unit; the central control unit is connected with the polymerized monomer feeding and diluting unit, the power driving unit, the heat exchange unit and the pressure control unit; the central control unit is connected with the catalyst feeding control unit, the initial polymerization monomer or the solvent feeding control unit. The utility model discloses mainly be to this characteristic of polymerization, develop the polymerization system that is suitable for strong heat release and viscosity fluctuation on a large scale that low-shear high circulation volume stirring and multilayer multitube inner coil heat exchanger combined together.
Description
Technical Field
The utility model relates to a exothermic technical field of polymerization especially relates to a heat transfer polymerization system in cauldron for strong exothermic polymerization.
Background
The polymer is a macromolecular compound having a molecular weight of more than 1000, which is formed by repeating a plurality of specific structural units through covalent bonds. The average value of the number of repeating units contained in the polymer is referred to as the degree of polymerization of the polymer. The different molecules of the same polymer do not have the same number of links, so that each polymer product essentially has a mixture of molecular weight distributions. The narrower the molecular weight distribution, the higher the quality of the product.
The synthesis reaction of the polymer has two types: one is called condensation polymerization (polycondensation), and the other is called addition polymerization (polyaddition).
The polycondensation reaction refers to a polymerization reaction in which monomers having two or more functional groups condense with each other to produce small molecule by-products (water, alcohol, ammonia, hydrogen halide, etc.) to produce a high molecular compound.
No low molecular substance is generated in the addition polymerization reaction process, the generated polymer has the same chemical composition with the raw material substance, and the relative molecular mass of the generated polymer is integral multiple of the relative molecular mass of the raw material.
The polymerization reaction is often accompanied by a large amount of reaction heat, if the reaction heat is not removed in time, the temperature in the kettle is over-temperature, the reaction temperature deviates from the normal reaction temperature, the product quality is influenced, and even the reaction over-temperature and high pressure can be caused in severe cases, so that safety accidents are caused. The physical property change in the polymerization reaction process is large (especially the viscosity change of materials is severe), and the working conditions of mass transfer and heat transfer are complex, so the mass transfer and heat transfer of the polymerization reaction are always engineering and technological problems in the industry.
In order to solve the heat transfer problem of the strongly exothermic polymerization reaction, the traditional method is to adopt an external circulation method and remove the reaction heat by a method of cooling and heat exchanging outside a reactor. The method has the advantages that the disadvantages of limited area of a heat exchanger in the reactor and limited flow of a heat exchange medium can be avoided, the heat release in the polymerization process can be completely removed, the temperature runaway and overpressure of the reactor are avoided, and the process safety is ensured. However, in the process of conveying materials by the circulating pump, the impeller of the pump can shear the materials at a high speed, so that the gel amount is increased easily, the polymer quality is reduced, and the subsequent filtration and purification are difficult.
In order to solve the problem, the patent provides an in-kettle heat exchange polymerization reaction system suitable for strong exothermic polymerization reaction.
SUMMERY OF THE UTILITY MODEL
Although the polymerization reaction process is usually accompanied by violent heat release and the viscosity of a system rises sharply, the working conditions of mass transfer and heat transfer are complex, and the difficulty of mass transfer and heat transfer is large. But in the polymerization reaction process, the viscosity of the materials is lower and the reaction heat is high at the early stage of the reaction; in the later stage of the reaction, the viscosity of the system is high and the reaction heat is low.
Aiming at the characteristic of polymerization reaction, the patent mainly develops a polymerization reaction system which combines low-shear high-circulation stirring and a multi-layer multi-pipe inner coil heat exchanger and is suitable for strong heat release and large-range fluctuation of viscosity. The stirring of low-shear high circulation volume improves the interior flow field of cauldron, improves the velocity of flow and the homogeneous mixing of material in the cauldron, improves molecular weight distribution, through the velocity of flow that improves the coil pipe region, improves heat transfer efficiency, through reducing the shearing of paddle to the material, reduces the formation of gel, reduces follow-up filtration degree of difficulty, improvement product yield. The monomer feeding is moved outside the kettle, and the mode of diluting outside the kettle is adopted, so that the mixing speed of the reaction monomer and the material is improved, and the reaction uniformity is improved. The mass transfer, heat transfer and formula integrated accurate control system is innovatively designed, the optimal temperature control curve of the reaction is realized, the gel production amount is reduced, the molecular weight distribution of the polymer is improved, and the product quality is improved.
The utility model provides a technical scheme as follows:
an in-kettle heat exchange polymerization reaction system for a strongly exothermic polymerization reaction, comprising:
the reaction kettle is internally provided with a stirring device, and a heat exchange coil is arranged between the inner side wall of the reaction kettle and the stirring device;
the polymerized monomer feeding and diluting unit is arranged at the outlets of a polymerized monomer feeding source and a diluting circulating pump of the reaction kettle;
a power drive unit disposed at the stirring device;
the heat exchange unit is arranged at the position of the heat exchange coil and the side wall of the reaction kettle;
the pressure control unit is arranged at an inert gas outlet of the reaction kettle and an inert gas inlet;
the catalyst feeding control unit is arranged at a catalyst inlet of the reaction kettle;
the system comprises an initial polymerization monomer or solvent feeding control unit, a polymerization monomer or solvent feeding control unit and a polymerization monomer feeding control unit, wherein the initial polymerization monomer or solvent feeding control unit is arranged at an initiator feeding port and a polymerization monomer feeding source of a reaction kettle;
the central control unit is connected with the polymerized monomer feeding and diluting unit, the power driving unit, the heat exchange unit and the pressure control unit; the central control unit is connected with the catalyst feeding control unit, the initial polymerization monomer or the solvent feeding control unit.
Preferably, the polymerized monomer feed dilution unit comprises:
the dilution mixer is provided with a first inlet and a second inlet, the first inlet is communicated with a dilution outlet of a polymerization kettle of the reaction kettle through a dilution circulating pump, the second inlet is communicated with a polymerization monomer source, a flow control device is arranged at the second inlet, the flow control device controls the flow of the polymerization monomer source through a valve, and a mixture outlet of the dilution mixer is communicated with a polymerization monomer feeding source of the reaction kettle;
a plurality of flow guide components are arranged in the dilution mixer.
Further, preferably, the dilution mixer is a venturi static mixer, the length of a throat of the venturi static mixer is 0.2 to 2 times, preferably 0.5 to 1 times, the diameter of the cross section of the second inlet and the diameter of the cross section of the mixture outlet, and the angle of the contraction section of the venturi static mixer is 24 to 40 degrees; the angle of the diffusion section of the venturi static mixer is 7-17 °.
Preferably, the stirring device comprises:
the power driving shaft is vertically and fixedly arranged in the reaction kettle;
multilayer stirring rake, every layer the stirring rake includes a plurality of paddles, the paddle with the power drive shaft passes through connecting rod fixed connection, the width of paddle is by keeping away from the one end of power drive shaft is to being close to the streamlined reduction gradually of one end of power drive shaft.
Further, preferably, the paddle is in a curved boot shape, the paddle is arranged in an inclined manner, and the inclined angle is 30-60 degrees relative to the horizontal plane;
the distance between every two adjacent stirring paddles is 0.6-2 times of the diameter of each paddle, and preferably 1-1.5 times of the diameter of each paddle; the diameter of the paddle is 6-20 times of that of the connecting rod; the diameter of the stirring paddle is 0.25-0.7 times of the inner diameter of the reaction kettle, and preferably 0.3-0.6 times.
Preferably, the heat exchange unit comprises:
the heat exchange device comprises a plurality of layers of heat exchange coil pipes, preferably 2-4 layers, each layer of heat exchange coil pipe comprises a plurality of heat exchange pipes, the plurality of heat exchange pipes are arranged in parallel, and each layer of heat exchange coil pipe is arranged in a staggered mode;
the outlet of the heat exchange coil is communicated with a refrigerant outlet and a heat medium outlet of the reaction kettle through a cold and heat medium outlet pipe;
the inlet of the heat exchange coil is communicated with a refrigerant inlet and a heat medium inlet of the reaction kettle through a cold heat medium inlet pipe;
the temperature control device is arranged at a refrigerant inlet and a heating medium inlet of the reaction kettle;
the reactor jacket is arranged on the outer side of the reaction kettle.
Further, preferably, the diameter of the heat exchange tube is 19-50 mm; the pitch of each layer of the heat exchange coil is 1.3-3 d; the distance between the heat exchange coil close to the inner wall of the reaction kettle and the inner wall of the reaction kettle is 50-200 mm; the number of each layer of heat exchange coil pipes is 3-10.
Preferably, flow control devices are arranged at the catalyst inlet and the starter feeding port, the inert gas discharging port and the inert gas inlet are communicated through a gas inlet pipe, and a pressure control device is arranged at the gas inlet pipe.
The utility model provides a pair of a heat transfer polymerization reaction system in cauldron for strong exothermic polymerization reaction can bring following beneficial effect:
the utility model discloses mainly be to this characteristic of polymerization, develop the polymerization system that is suitable for strong heat release and viscosity fluctuation on a large scale that low-shear high circulation volume stirring and multilayer multitube inner coil heat exchanger combined together. The stirring of low-shear high circulation volume improves the interior flow field of cauldron, improves the velocity of flow and the homogeneous mixing of material in the cauldron, improves molecular weight distribution, through the velocity of flow that improves the coil pipe region, improves heat transfer efficiency, through reducing the shearing of paddle to the material, reduces the formation of gel, reduces follow-up filtration degree of difficulty, improvement product yield. The monomer feeding is moved outside the kettle, and the mode of diluting outside the kettle is adopted, so that the mixing speed of the reaction monomer and the material is improved, and the reaction uniformity is improved. The mass transfer, heat transfer and formula integrated accurate control system is innovatively designed, the optimal temperature control curve of the reaction is realized, the gel production amount is reduced, the molecular weight distribution of the polymer is improved, and the product quality is improved.
Drawings
The above features, technical characteristics, advantages and modes of realisation of an in-kettle heat exchange polymerization system for strongly exothermic polymerizations will be further described in the following, in a clearly understandable manner, with reference to the accompanying drawings, which illustrate preferred embodiments.
FIG. 1 is a schematic structural view of an in-kettle heat exchange polymerization system for a strongly exothermic polymerization reaction of the present invention;
FIG. 2 is a schematic diagram of the venturi static mixer of the present invention;
FIG. 3-A is a cross-sectional view of the multi-layer coil of the present invention;
FIG. 3-B is a schematic view of the heat exchange medium entering the inlet of a multi-tube parallel single layer heat exchange coil;
fig. 4 is a schematic structural diagram of the stirring device of the present invention.
The reference numbers illustrate:
the device comprises a reaction kettle 1, a stirring device 2, a connecting rod 2.1, a blade 2.2, a power driving shaft 2.3, a heat exchange coil 3, a heat exchange tube 3.1, a refrigerant outlet 3.2, a heat medium outlet 3.3, a refrigerant inlet 3.4, a heat medium inlet 3.5, a central control unit 4, a dilution circulating pump 5, a dilution mixer 6, a polymerization monomer feed source 7, a flow control device 8, a pressure control device 9, a temperature control device 10, a valve 11, an initiator feed inlet 12, a catalyst inlet 13, an inert gas outlet 14, an inert gas inlet 15, a polymerization kettle diluent outlet 16, a reactor jacket 17, a mixture outlet 6.1, a first inlet 6.2, a second inlet 6.3 and a flow guide member 6.4.
Detailed Description
In order to more clearly illustrate embodiments of the present invention or technical solutions in the prior art, specific embodiments of the present invention will be described below with reference to the accompanying drawings. It is obvious that the drawings in the following description are only examples of the invention, and that for a person skilled in the art, other drawings and embodiments can be obtained from these drawings without inventive effort.
For the sake of simplicity, the drawings only schematically show the parts relevant to the present invention, and they do not represent the actual structure of the product.
[ example 1 ]
As shown in fig. 1, example 1 discloses an in-kettle heat exchange polymerization reaction system for a strongly exothermic polymerization reaction, which specifically comprises:
a reaction kettle 1, wherein a stirring device 2 is arranged in the reaction kettle 1, and a heat exchange coil 3 is arranged between the inner side wall of the reaction kettle 1 and the stirring device 2;
the polymerization monomer feeding dilution unit is arranged at the outlets of a polymerization monomer feeding source 7 and a dilution circulating pump 5 of the reaction kettle 1 and is used for diluting the feeding of the polymerization monomer;
the power driving unit is arranged at the stirring device 2 and is used for driving the stirring device 2 to rotate;
the heat exchange unit is arranged at the position of the heat exchange coil 3 and the side wall of the reaction kettle and is used for exchanging heat for the materials in the reaction kettle 1;
the pressure control unit is arranged at an inert gas outlet 14 and an inert gas inlet 15 of the reaction kettle 1 and is used for detecting the pressure value in the reaction kettle 1 and adjusting the flow of the inert gas;
the catalyst feeding control unit is arranged at a catalyst inlet of the reaction kettle 1 and is used for controlling the flow of the catalyst;
the initial polymerization monomer or solvent feeding control unit is arranged at an initiator feeding port 12 and a polymerization monomer feeding source 7 of the reaction kettle 1 and is used for controlling the flow of the initial polymerization monomer or solvent feeding;
the central control unit 4 is connected with the polymerized monomer feeding dilution unit, the power driving unit, the heat exchange unit and the pressure control unit and is used for controlling the on-off and operation regulation of the polymerized monomer feeding dilution unit, the power driving unit, the heat exchange unit and the pressure control unit; the central control unit 4 is connected with the catalyst feeding control unit and the initial polymerization monomer or solvent feeding control unit, and is used for controlling the starting and the stopping of the catalyst feeding control unit and the initial polymerization monomer or solvent feeding control unit and controlling the proportion and the flow rate of the catalyst and the initial polymerization monomer or solvent.
Specifically, flow control devices 8 are arranged at the catalyst inlet and the starter feeding port, an inert gas outlet 14 and an inert gas inlet 15 are communicated through a gas inlet pipe, and a pressure control device 9 is arranged at the gas inlet pipe.
The flow control device consists of a flowmeter, an electromagnetic valve and a controller, and can realize the functions of measuring the flow and controlling the flow.
The pressure control device consists of a pressure gauge, an electromagnetic valve and a controller, and can realize the functions of measuring the pressure and controlling the pressure.
The pressure control unit maintains the stability of the pressure in the reaction kettle 1 through PIC (pressure control device 9), if the pressure is reduced, the pressure control device 9 controls the valve 11 at the inert gas inlet 15 to be opened, the valve 11 at the inert gas outlet 14 to be closed, the inert gas feeding is started in a linkage manner, if the pressure value exceeds a preset range, the pressure control device 9 controls the valve 11 at the inert gas inlet 15 to be closed, the valve 11 at the inert gas outlet 14 to be opened, and the inert gas feeding is started in a linkage manner.
In order to prevent combustion and explosion accidents, inert gas is first introduced into the reaction vessel 1 to replace the reaction vessel 1 with inert gas. After replacement, the central control unit 4 controls the monomer feeding and diluting unit and the catalyst feeding control unit to automatically add the initial monomer or the solvent and the catalyst according to the formula, and simultaneously starts the power driving unit, the heat exchange unit and the pressure control unit to uniformly mix the materials in the reaction kettle 1 and maintain the materials within the range of the designed temperature and pressure value.
When the temperature and the pressure in the reaction kettle 1 reach the preset initial conditions of the polymerization reaction, the polymerized monomer feeding and diluting unit is started to dilute the polymerized monomer and inject the diluted polymerized monomer into the reaction kettle 1, the diluted polymerized monomer is rapidly and uniformly mixed with the initial monomer or a reaction liquid formed by a solvent and a catalyst under the stirring action of the power driving unit to generate the polymerization reaction, and the heat generated by the polymerization reaction is removed through the exchange of a cooling medium and a heating medium in the heat exchange unit.
The central control unit 4 controls the polymerized monomer feeding dilution unit, the power driving unit, the heat exchange unit, the pressure control unit, the catalyst feeding control unit and the initial polymerized monomer or solvent feeding control unit to automatically carry out the whole polymerization reaction process, thereby ensuring the reaction consistency among different batches and the stability of product indexes.
[ example 2 ]
As shown in fig. 2, the present embodiment further discloses, on the basis of embodiment 1, that the polymerized monomer feed dilution unit includes:
the specific structure of the dilution mixer 6 is shown in fig. 2, the dilution mixer 6 is provided with a first inlet 6.2 and a second inlet 6.3, the first inlet 6.2 is communicated with a polymeric kettle diluent outlet 16 of the reaction kettle 1 through a dilution circulating pump 5, the second inlet 6.3 is communicated with a polymeric monomer feed source 7, a flow control device 8 is arranged at the second inlet 6.3, the flow control device 8 controls the flow of the polymeric monomer feed source 7 through a valve 11, and a mixture outlet of the dilution mixer is communicated with a polymeric monomer feed inlet of the reaction kettle 1;
a plurality of flow guiding members 6.4 are arranged in the dilution mixer 6.
The utility model discloses continuous feeding monomer among the reaction unit adopts the ware to dilute the feeding outward, takes out a small part material promptly from reation kettle 1, carries out the ware extrinsic cycle, makes it and polymerization monomer mix through diluting mixer 6. In the embodiment, when the temperature and the pressure in the reaction kettle 1 reach the preset initial conditions of the polymerization reaction, the dilution circulating pump 5 is started, the polymerization monomer is uniformly mixed with the circulating diluent through the dilution mixer 6, and then the mixture is injected into the reaction kettle 1, wherein the flow ratio of the circulating diluent to the monomer is 10: 1-200: 1, and the optimal ratio is 20: 1-100: 1. Too large a dilution ratio results in too large a circulating material and an increased gel production rate; the dilution ratio is too small to facilitate uniform mixing of the monomer and the material.
Specifically, the dilution mixer 6 is a venturi type static mixer, the length of a throat of the venturi type static mixer is 0.2-2 times of the diameter of the cross section of the second inlet and the mixture outlet 6.1, the optimal value is 0.5-1.0 times, if the length is too long, the mixture is easy to be insufficiently mixed, and if the length is too short, the resistance is too large;
the angle of the contraction section of the Venturi type static mixer is 24-40 degrees; the angle of the diffusion section of the Venturi type static mixer is 7-17 degrees, and the fluid is easy to peel off due to too large diffusion angle.
In this embodiment, the mixer is a venturi type static mixer with a built-in flow guide member 6.4, which is arranged at an outlet of the dilution circulation pump 5, the structure of the venturi type static mixer is shown in fig. 2, the diluent enters the venturi type static mixer through a venturi contraction section inlet, namely a first inlet, is mixed with a polymerized monomer from a side wall in an acceleration process, the entrained polymerized monomer enters a throat pipe after being accelerated, the mixed monomer is further accelerated in the throat pipe, the mixed monomer enters a diffusion section and is gradually decelerated to a normal flow velocity, and a streamline flow guide member 6.4 is added to the diffusion section to avoid vortex and flow field stripping.
[ example 3 ]
As shown in fig. 4, this embodiment specifically discloses the structure of the stirring device 2 in addition to embodiment 1.
The method comprises the following steps:
the power driving shaft 2.3 is vertically and fixedly arranged at the center of the kettle body of the reaction kettle 1;
each layer of the multilayer stirring paddles comprises a plurality of paddles 2.2, one ends of the paddles 2.2 are fixedly connected with the power driving shaft 2.3 through a connecting rod 2.1, and the width of the paddles 2.2 is gradually reduced from one end far away from the power driving shaft 2.3 to one end close to the power driving shaft 2.3 in a streamline mode.
After the power driving system starts the stirring motor, the power driving shaft 2.3 connected with the stirring motor drives the blade 2.2 to rotate, so that a large axial driving force is easy to generate, the shearing response of the edge of the blade 2.2 to liquid is small, and the vortex generation is favorably reduced. The radial mixing of the materials in the reaction vessel 1 is realized by the radial speed generated by the blades 2.2 when rotating around the power driving shaft 2.3 and the baffle effect of the heat exchange coil 3 on the axial flow. The stirring speed is automatically controlled by a power driving system according to a detection signal of the viscosity of the liquid in the reaction kettle 1 and a reaction sequence control logic.
The paddle 2.2 is a curved surface boot shape, the outer end of the paddle 2.2 is an elliptical arc with the ratio of the long axis to the short axis close to 2, the paddle 2.2 is obliquely arranged, and the inclination angle is 30-60 degrees with the horizontal plane.
As the reaction proceeds, the average molecular weight of the materials in the reaction kettle 1 is increased, the heat release of the reaction is decreased, the viscosity of the materials is increased, and the reaction rate is reduced. In order to satisfy the requirement of polymerization mass transfer, heat transfer, the utility model discloses a 4 three-dimensional paddle of formula of turning over behind the leaf stirs, and paddle 2.2 turns over the angle after in proper order for 40 ~ 90, and paddle 2.2 is curved surface boots shape paddle, and paddle 2.2 outer end is the elliptical arc that ratio of major and minor axis is close 2, and paddle 2.2 is the streamlined increase gradually of width from inside to outside. The blade with the structure can enable the fluid to generate faster flow speed, the flow speed range of the fluid around the blade 2.2 reaches 1-3 m/s, and is 20% higher than that of the common blade, so that the blade can generate larger pumping capacity, and the mass transfer efficiency and the heat exchange efficiency are effectively improved.
The distance between the adjacent stirring paddles is 0.6-2 times of the diameter of 2.2 of the paddle, the optimal value of the distance is 1-1.5 times, and if the distance is too short, not only is the energy consumption increased, but also the fluid is over-sheared; the diameter of the paddle 2.2 is 6-20 times of that of the connecting rod; the diameter of the stirring paddle is 0.25-0.7 times of the inner diameter of the reaction kettle 1, the optimal value of the diameter is 0.3-0.6 times, and the stirring of the structural design can enable the flow velocity of fluid in the kettle to be more uniform. In the early stage of high exothermic reaction, the self-control adjusting rotating speed is improved, the heat exchange coil 3 is in an outer pipe liquid flow field of 0.8-2 m/s, and the heat exchange efficiency between the material and the heat exchange medium is improved due to high flow velocity. In the later stage of the high-heat-release reaction, the average molecular weight of the materials is increased, the viscosity is increased, the reaction heat release is reduced, the heat exchange coil 3 is positioned in an outer-pipe liquid flow field of 0.5-1 m/s, and the wall-hanging pollution of the high-viscosity materials on the inner wall of the reaction kettle 1 and the outer surface of the heat exchange coil 3 is reduced.
The power driving system in the embodiment can adapt to the requirements of mass transfer and heat exchange of the reaction by controlling the rotating speed of the stirring device 2 according to the reaction kinetic data and the viscosity change of the materials.
[ example 4 ]
As shown in fig. 1, in embodiment 4, on the basis of embodiments 1 to 3, embodiment 4 further includes a heat exchange unit, and the heat exchange unit includes:
2-4 layers of heat exchange coil pipes 3, wherein each layer of heat exchange coil pipe 3 comprises a plurality of heat exchange pipes 3.1, the plurality of heat exchange pipes 3.1 are arranged in parallel, and the arrangement schematic diagram of the single-layer heat exchange pipes 3.1 with multiple parallel pipes is shown in a figure 3-B; each layer of heat exchange coil 3 is arranged in a staggered way as shown in figure 3-A, and mass transfer and heat transfer effects are improved by matching with stirring; the advantage of setting up like this can increase heat exchange medium's flow, satisfies the demand of big heat transfer volume and reduces the resistance of heat transfer.
An outlet of the heat exchange coil 3 is communicated with a refrigerant outlet 3.2 and a heat medium outlet 3.3 of the reaction kettle 1 through a cold heat medium outlet pipe;
the inlet of the heat exchange coil 3 is communicated with a refrigerant inlet 3.4 and a heat medium inlet 3.5 of the reaction kettle 1 through a cold heat medium inlet pipe;
the reactor jacket 17 is arranged outside the reaction kettle 1, and the reactor jacket 17 has a small heat transfer area and can play a role in assisting the heat transfer of the inner coil.
The temperature control device 10 is arranged at the positions of a refrigerant inlet 3.4 and a heating medium inlet 3.5 of the reaction kettle 1, and the temperature control device 10 is arranged at the positions of a heating medium inlet 3.4 and a heating medium inlet 3.5 of the reaction kettle 1. The temperature control device 10 controls the temperature of the reaction kettle by controlling the amount of the heat exchange medium entering the reactor jacket 17 and the heat exchange coil 3, and can realize the functions of measuring the temperature and controlling the temperature.
The diameter of the heat exchange tube 3.1 is 19-50 mm, the diameter is too small, the cleaning and the maintenance are difficult, the diameter is too large, the boundary layer is thick, the thermal resistance is large, and the heat transfer effect is poor; the pitch of each layer of heat exchange coil 3.1 is 1.3-3 d, the distance is too small, dead zones are easily caused, mass transfer and heat transfer effects of the reaction are affected, the distance is too large, short circuit of fluid is easily caused, and the heat transfer effect is poor; the distance between the heat exchange coil 3 close to the inner wall of the reaction kettle 1 and the inner wall of the reaction kettle 1 is 50-200 mm, and too large distance can cause poor heat exchange effect of liquid between the heat exchange coil 3 and the abdominal wall, too small distance, slow flow velocity of fluid outside the coil, small heat transfer coefficient and poor heat exchange effect; the number of the heat exchange tubes 3.1 of each layer of the heat exchange coil 3 is related to the amount of the required heat exchange medium, and the optimal value range is 3-10.
The heat exchange system detects the reaction temperature of the reaction kettle 1 through a TIC (temperature control detection device 10) to adjust the flow of the heat exchange medium, so that the temperature in the reaction kettle 1 is stabilized within a design range.
It should be noted that the above embodiments can be freely combined as necessary. The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (8)
1. An in-kettle heat exchange polymerization reaction system for a strongly exothermic polymerization reaction, comprising:
the reaction kettle is internally provided with a stirring device, and a heat exchange coil is arranged between the inner side wall of the reaction kettle and the stirring device;
the polymerized monomer feeding and diluting unit is arranged at the outlets of a polymerized monomer feeding source and a diluting circulating pump of the reaction kettle;
a power drive unit disposed at the stirring device;
the heat exchange unit is arranged at the position of the heat exchange coil and the side wall of the reaction kettle;
the pressure control unit is arranged at an inert gas outlet of the reaction kettle and an inert gas inlet;
the catalyst feeding control unit is arranged at a catalyst inlet of the reaction kettle;
the system comprises an initial polymerization monomer or solvent feeding control unit, a polymerization monomer or solvent feeding control unit and a polymerization monomer feeding control unit, wherein the initial polymerization monomer or solvent feeding control unit is arranged at an initiator feeding port and a polymerization monomer feeding source of a reaction kettle;
the central control unit is connected with the polymerized monomer feeding and diluting unit, the power driving unit, the heat exchange unit and the pressure control unit;
the central control unit is connected with the catalyst feeding control unit, the initial polymerization monomer or the solvent feeding control unit.
2. The system of claim 1, wherein the dilution unit comprises:
the dilution mixer is provided with a first inlet and a second inlet, the first inlet is communicated with a dilution outlet of a polymerization kettle of the reaction kettle through a dilution circulating pump, the second inlet is communicated with a polymerization monomer source, a flow control device is arranged at the second inlet, the flow control device controls the flow of the polymerization monomer source through a valve, and a mixture outlet of the dilution mixer is communicated with a polymerization monomer feeding source of the reaction kettle;
a plurality of flow guide components are arranged in the dilution mixer.
3. The system of claim 2, wherein:
the dilution mixer is a Venturi static mixer, the length of a throat pipe of the Venturi static mixer is 0.2-2 times of the diameter of the section of the second inlet and the diameter of the section of the mixture outlet, and the angle of a contraction section of the Venturi static mixer is 24-40 degrees; the angle of the diffusion section of the venturi static mixer is 7-17 °.
4. The system of claim 1, wherein the stirring means comprises:
the power driving shaft is vertically and fixedly arranged in the reaction kettle;
multilayer stirring rake, every layer the stirring rake includes a plurality of paddles, the paddle with the power drive shaft passes through connecting rod fixed connection, the width of paddle is by keeping away from the one end of power drive shaft is to being close to the streamlined reduction gradually of one end of power drive shaft.
5. The system of claim 4, wherein:
the paddle is in a curved surface boot shape, the paddle is arranged in an inclined mode, and the inclined angle is 30-60 degrees relative to the horizontal plane;
the distance between every two adjacent stirring paddles is 0.6-2 times of the diameter of each paddle; the diameter of the paddle is 6-20 times of that of the connecting rod; the diameter of the stirring paddle is 0.25-0.7 times of the inner diameter of the reaction kettle.
6. The system of claim 1, wherein the heat exchange unit comprises:
the heat exchange device comprises a plurality of layers of heat exchange coil pipes, a heat exchanger and a heat exchanger, wherein each layer of heat exchange coil pipe comprises a plurality of heat exchange pipes which are arranged in parallel, and each layer of heat exchange coil pipe is arranged in a staggered manner;
the outlet of the heat exchange coil is communicated with a refrigerant outlet and a heat medium outlet of the reaction kettle through a cold and heat medium outlet pipe;
the inlet of the heat exchange coil is communicated with a refrigerant inlet and a heat medium inlet of the reaction kettle through a cold heat medium inlet pipe;
the temperature control device is arranged at a refrigerant inlet and a heating medium inlet of the reaction kettle;
the reactor jacket is arranged on the outer side of the reaction kettle.
7. The system of claim 6, wherein:
the diameter of the heat exchange tube is 19-50 mm; the pitch of each layer of the heat exchange coil is 1.3-3 d; the distance between the heat exchange coil close to the inner wall of the reaction kettle and the inner wall of the reaction kettle is 50-200 mm; the number of the heat exchange tubes of each layer of the heat exchange coil is 3-10.
8. The system of claim 1, wherein:
the catalyst inlet and the starter feed inlet are respectively provided with a flow control device, the inert gas outlet and the inert gas inlet are communicated through a gas inlet pipe, and the gas inlet pipe is provided with a pressure control device.
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| CN201921272629.6U CN210545133U (en) | 2019-08-07 | 2019-08-07 | In-kettle heat exchange polymerization reaction system for strong exothermic polymerization reaction |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110302736A (en) * | 2019-08-07 | 2019-10-08 | 上海蓝科石化环保科技股份有限公司 | Exchange heat polymerization reaction system and method in a kind of kettle for strongly exothermic polymerization reaction |
| CN116159509A (en) * | 2021-11-25 | 2023-05-26 | 中国石油化工股份有限公司 | System and method for continuous industrial production of high molecular weight crude PGA |
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2019
- 2019-08-07 CN CN201921272629.6U patent/CN210545133U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110302736A (en) * | 2019-08-07 | 2019-10-08 | 上海蓝科石化环保科技股份有限公司 | Exchange heat polymerization reaction system and method in a kind of kettle for strongly exothermic polymerization reaction |
| CN110302736B (en) * | 2019-08-07 | 2024-06-21 | 上海蓝科石化环保科技股份有限公司 | In-kettle heat exchange polymerization reaction system and method for strong exothermic polymerization reaction |
| CN116159509A (en) * | 2021-11-25 | 2023-05-26 | 中国石油化工股份有限公司 | System and method for continuous industrial production of high molecular weight crude PGA |
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