Multi-channel full-mixed-flow injection loop reaction device

Abstract

The invention discloses a multi-channel full-mixed-flow injection loop reaction device, which comprises a reactor, an injector, an injection loop, a gas-liquid separation net and a plurality of liquid-liquid mixers, and the plurality of liquid-liquid mixers are distributed in the reactor along different heights under liquid of the reactor. And a plurality of liquid-liquid mixing channels are connected to the spraying loop so as to be correspondingly connected to the liquid-liquid mixers. According to the invention, a plurality of circulation channels are additionally arranged on a jet loop, so that uniform distribution of continuous phase materials and dispersed phase materials in the reactor is realized, all nodes in the reactor have the same reaction probability, and the material distribution uniformity and polymerization degree consistency are improved; besides, a rapid separation device for separating gas from liquid is additionally arranged in the reactor disclosed by the invention, so that non-reactive gas carried by the ejector can be efficiently and rapidly subjected to gas-liquid separation from a liquid material so as to enter an upper gas-phase space of the reactor; therefore, the problems of production efficiency reduction and potential safety hazards caused by rapid reduction and even paralysis of the heat exchange system of the reactor are avoided.

Description

Technical Field

[0001] The invention relates to the technical field of jet loop reaction devices, and in particular to a multi-channel full mixed flow jet loop reaction device. Background Art

[0002] The jet loop process is widely used in processes such as ethoxylation (ie: ethoxylation, propoxylation), alkylation, polymerization, hydrogenation, etc. Compared with processes such as stirring, spraying, and pipeline reactors, the jet loop has the highest mass transfer efficiency and has great advantages in terms of product quality purity and by-product control. However, the jet loop reaction device has the following two obvious defects in actual applications, which limit its widespread promotion and application in various processes. For example, the actual application ratio of the jet loop in the ethoxylation reaction is less than 20%, and the application ratio in other fields is slightly higher.

[0003] (1) One of the drawbacks of the existing injection loop reactor is the problem of uniformity of the material circulation cycle inside the reactor:

[0004] In order to enhance the mass transfer and reaction effect of the jet loop reactor, the jets are equipped with longer jet pipes, such as Figure 1 As shown in the figure, the material enters the reactor from the bottom and is pressurized by the pump. Then, it is ejected from the injection pipe (ejector) at point ① to form a cycle. Due to the difference in material potential energy, the material from point ① downward in the reactor can circulate rapidly, with a cycle period of about 0.5 to 2.0 minutes, while the material in the area above point ① (for example, point ②) tends to be static, with a cycle period of 2.0 to 20 minutes or even no circulation.

[0005] To solve Figure 1 The above problems were improved by adding a double loop, such as Figure 2 As shown, it includes a first ejector (large ejector) and a second ejector (small ejector). To ensure that the second ejector is as close to the liquid surface as possible, the second ejector needs to be as small as possible, so that its circulation capacity and reaction capacity are relatively weak, and the mass transfer in the reactor changes as follows: the material at point ① in the reactor circulates rapidly downward, with a circulation period of about 0.5 to 2.0 minutes, the material circulation period at point ② in the reactor is about 2.0 to 15 minutes, and the circulation period at point ③ is about 15 minutes to no circulation.

[0006] In addition, some researchers have achieved consistency in the material circulation cycle in the reactor by increasing the installation height of the ejector. However, the increase in the installation height of the ejector has increased the construction cost and the operating cost has increased exponentially. At the same time, when the material flows horizontally from the top to the bottom of the reactor, the concentrations of the continuous phase material and the dispersed phase material in the reactor are inconsistent, and even the dispersed phase reacts completely in the later stage, wasting the kinetic energy of the system. It will also cause uneven material distribution and degree of polymerization.

[0007] (2) Another drawback of the existing injection loop reaction device is the negative effect caused by the ejector carrying non-reactive gas:

[0008] The ejector is specifically a Venturi ejector. The core function of the ejector circuit is to suck the dispersed phase material in the gas phase into the system through negative pressure under the action of the liquid continuous phase to achieve efficient mass transfer, dispersion and reaction. Due to the material safety requirements, a certain amount of inert gas (such as nitrogen N2) needs to be added to the general system as a safety protection. When the ejector sucks the gas phase dispersed phase material, it also brings N2 into the system. The dispersed phase material reacts with the continuous phase material in the ejector to form a new liquid product, while N2 cannot react and is ejected from the ejector pipe outlet with the material. Under the action of the high flow rate of the material, it is difficult to separate N2. Only a part of it is separated from the liquid and re-enters the upper gas phase space of the reactor, while most of it continues to circulate with the liquid. In particular, as the degree of polymerization increases, the viscosity increases, and the amount of N2 carried in the material becomes larger and larger. When the material viscosity reaches 50p, about 90% of N2 continues to circulate with the material.

[0009] Because the liquid material carries a large amount of N2, the thermal conductivity of the heat exchanger drops sharply. When 90% N2 circulates with the material, the heat exchange efficiency drops by more than 80%. The reaction efficiency decreases proportionally with the heat exchange efficiency. The process capacity is basically lost and safety cannot be guaranteed. Summary of the invention

[0010] 1. Technical issues to be resolved

[0011] In view of the deficiencies in the prior art, the present invention provides a multi-channel full mixed flow injection loop reaction device that can solve the above technical problems.

[0012] (II) Technical solution

[0013] In order to solve the above technical problems, the present invention provides the following technical solutions: a multi-channel fully mixed flow jet loop reaction device, comprising a reactor, an ejector and an ejection loop, the ejector is arranged at the top of the barrel of the reactor, the ejection loop connects the feed port of the ejector and the discharge port of the reactor, the ejection loop is provided with a reaction circulation pump, the multi-channel fully mixed flow jet loop reaction device also comprises a gas-liquid separation network and a plurality of liquid-liquid mixers, the plurality of liquid-liquid mixers are distributed in the reactor at different heights under the liquid of the reactor, a plurality of liquid-liquid mixing channels are connected to the ejection loop to be correspondingly connected to each liquid-liquid mixer, the gas-liquid separation network is arranged in the reactor and close to the bottom of the barrel of the reactor.

[0014] Preferably, the injection circuit is a single circuit or multiple circuits.

[0015] Preferably, when the injection circuit is a multi-circuit circuit, a plurality of liquid-liquid mixing channels are connected to any circuit or multiple circuits of the injection circuit.

[0016] Preferably, the multiple liquid-liquid mixers adopt one or a combination of rotating nozzles, multi-channel multi-directional nozzles, and ejectors.

[0017] Preferably, the surface of the gas-liquid separation net is made of hydrophobic material or coated with a hydrophobic coating.

[0018] Preferably, the gas-liquid separation net comprises a vertical separation net portion and a separation net bottom, the vertical separation net portion is arranged close to the cylinder side wall of the reactor, and the separation net bottom is arranged close to the cylinder bottom of the reactor.

[0019] Preferably, the mesh diameter of the vertical portion of the separation net is 1 μm to 800 μm, and the mesh diameter of the bottom of the separation net is 0.1 mm to 5 mm.

[0020] Preferably, the bottom of the separation net is in an inverted arc shape or a downward cone shape.

[0021] Preferably, the gas-liquid separation network adopts a non-flat structure, and the injection loop is also provided with a circulating heat exchanger.

[0022] Preferably, the injector comprises a first injection tube body and a second injection tube body, wherein the first injection tube body and the second injection tube body are both in the shape of long strips, the length of the first injection tube body is longer than the length of the second injection tube body, the bottom end of the first injection tube body is at the bottom end in the reactor, and the bottom end of the second injection tube body is at the top end in the reactor.

[0023] (III) Beneficial effects

[0024] Compared with the prior art, the present invention provides a multi-channel fully mixed flow injection loop reaction device, which has the following beneficial effects: (1) The present invention adds a plurality of circulation channels (liquid-liquid mixing channels) to the injection loop, and adds a plurality of submerged mixing facilities (liquid-liquid mixers) on the basis of the original above-liquid gas-liquid reaction loop, so that the materials in the reactor are formed into a fully mixed flow form, and the continuous phase materials and the dispersed phase materials in the reactor are evenly distributed, and each node in the reactor has the same reaction probability, thereby improving the uniformity of material distribution and the consistency of polymerization degree, and achieving the consistency of the material circulation cycle in the reactor; (2) A rapid separation device (gas-liquid separation network) for separating gas from liquid is added to the reactor of the present invention, which can efficiently and quickly separate the non-reactive gases such as N2 carried by the injector from the liquid material to enter the upper gas phase space of the reactor, thereby avoiding the problems of decreased production efficiency and potential safety hazards caused by the rapid decrease or even paralysis of the reactor heat exchange system capacity. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Figure 1 It is a structural schematic diagram of a single-loop injection loop reaction device in the prior art; Figure 2It is a structural schematic diagram of a double-loop injection loop reaction device in the prior art; Figure 3 It is a structural schematic diagram of a first embodiment of a multi-channel full mixed flow injection loop reaction device of the present invention; Figure 4 This is a schematic diagram of CFD simulation of material distribution in the reactor of the present invention; Figure 5 It is a schematic diagram of the structure of the gas-liquid separation network in the first embodiment of the multi-channel full mixed flow injection loop reaction device of the present invention; Figure 6 It is a structural schematic diagram of the second embodiment of the multi-channel full mixed flow injection loop reaction device of the present invention (only one liquid-liquid mixing channel is shown and the gas-liquid separation network is not shown); Figure 7 It is a structural schematic diagram of a third embodiment of a multi-channel full mixed flow injection loop reaction device of the present invention; Figure 8 for Figure 7 A schematic diagram of the structure of the first suspension ball; Fig. 9 for Figure 7 Schematic diagram of the structure of the second suspension ball.

[0031] The numbers in the figure are: 1 reactor, 2 ejector, 3 reaction circulation pump, 4 circulation heat exchanger, 5 gas-liquid separation network, 6 liquid-liquid mixer, 7 separation network vertical part, 8 separation network bottom, 9 pressure detector, 10 temperature detector, 11 preprocessor, 12 pre-reaction circulation pump. DETAILED DESCRIPTION

[0032] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0033] The present invention provides a multi-channel fully mixed flow jet loop reaction device, which can be applied to processes such as ethylene propoxylation, alkylation, polymerization, and hydrogenation to increase efficiency and achieve narrow distribution. The multi-channel fully mixed flow jet loop reaction device comprises a reactor 1, an ejector 2, and an ejection loop. The ejector 2 is arranged at the top of the cylinder of the reactor 1. The ejection loop connects the feed port of the ejector 2 and the discharge port of the reactor 1. The ejection loop is provided with a reaction circulation pump 3 and a circulation heat exchanger 4. In the above manner, the material is circulated in the reactor 1. The ejector 2 can specifically adopt an ejector of the prior art such as a Venturi ejector. The reactor 1, the ejector 2, the reaction circulation pump 3, the circulation heat exchanger 4, etc. of the present invention are all prior art and will not be described in detail here.

[0034] In addition, the multi-channel fully mixed flow injection loop reaction device of the present invention also includes a gas-liquid separation network 5 and a plurality of liquid-liquid mixers 6. The plurality of liquid-liquid mixers 6 are distributed in the reactor 1 at different heights below the liquid of the reactor 1. The injection loop is connected to a plurality of liquid-liquid mixing channels to be connected to each liquid-liquid mixer 6 accordingly. The gas-liquid separation network 5 is arranged in the reactor 1 and close to the bottom of the cylinder of the reactor 1.

[0035] The injection circuit is a single circuit or multiple circuits (for example, a double circuit, a triple circuit, etc.). It can be understood that when the injection circuit is a single circuit, there is a corresponding injector 2 arranged at the top of the cylinder of the reactor 1; when the injection circuit is a double circuit, there are correspondingly two injectors 2 arranged at the top of the cylinder of the reactor 1.

[0036] When the injection circuit is a multi-circuit circuit, a plurality of liquid-liquid mixing channels can be connected to any circuit or multiple circuits of the injection circuit.

[0037] like Figure 3 As shown, in the first embodiment of the multi-channel full mixed flow injection loop reaction device of the present invention, the injection loop is a single loop, including an injector 2 and two liquid-liquid mixers 6. Accordingly, two liquid-liquid mixing channels are connected to the injection loop to be connected to the two liquid-liquid mixers 6 accordingly.

[0038] Multiple liquid-liquid mixers 6 can adopt one or more combinations of rotary nozzles, multi-channel multi-directional nozzles, ejectors, and jet nozzles in the prior art; for example: the two liquid-liquid mixers 6 in this embodiment both adopt rotary nozzles, or one liquid-liquid mixer 6 adopts a multi-channel multi-directional nozzle and the other liquid-liquid mixer 6 adopts an ejector, and no excessive restrictions are made here.

[0039] It can be understood that when the liquid level of the reaction liquid in the reactor 1 is lower than the position of the liquid-liquid mixer 6, gas-liquid collision, contact and reaction can be achieved; when the liquid level is higher than the liquid-liquid mixer 6, the liquid-liquid mixer 6 ejects high-flow rate liquid to quickly realize turbulent flow of the liquid in the reactor 1 in different directions, so that the liquid in the reactor 1 is in a similar turbulent stirring effect, driving the high-concentration dispersed phase (EO / PO) material at the outlet of the ejector 2 to be evenly distributed in the reactor 1 in about 10 seconds, effectively utilizing the liquid phase space of the reactor, accelerating the reaction and improving the reaction uniformity. The CFD simulation of material distribution in the reactor is shown in Figure 4 .

[0040] Preferably, the surface of the gas-liquid separation net 5 is made of hydrophobic material, or the surface of the gas-liquid separation net 5 is coated with a hydrophobic coating, so that the gas-liquid separation net 5 can better adapt to the stable operation of the reaction materials and realize the rapid separation and aggregation of gases such as nitrogen N2. In addition, preferably, the gas-liquid separation net 5 adopts a non-flat structure design, which is conducive to reducing the driving force of the flowing liquid on the gas and accelerating the gas aggregation efficiency.

[0041] In this embodiment, the gas-liquid separation net 5 includes a separation net vertical portion 7 and a separation net bottom 8 connected to each other, the separation net vertical portion 7 is arranged close to the cylinder side wall of the reactor 1, and the separation net bottom 8 is arranged close to the cylinder bottom of the reactor 1. Among them, the separation net bottom 8 can be installed at the connection between the cylinder bottom and the head of the reactor 1. In this embodiment, the separation net bottom 8 is in a downward cone shape, and in other embodiments, the separation net bottom 8 can also be in an inverted arc shape.

[0042] The bottom 8 of the separation net can guide and gather the separated N2 and other gases upward, while increasing the flow area to reduce the impact on liquid circulation; and the vertical part of the separation net (three-dimensional separation net) 7 is installed as close as possible to the side wall of the cylinder of the reactor 1 to reduce the impact on the turbulence of the reaction liquid. The vertical part 7 of the separation net will gather the gas separated by the bottom 8 of the separation net and the newly captured liquid to form larger bubbles and finally escape from the liquid to the upper gas phase space of the reactor 1. In order to meet the requirements of gas-liquid separation and liquid flow, the mesh diameter of the vertical part 7 of the separation net is preferably 1μm to 800μm, and the mesh diameter of the bottom 8 of the separation net is preferably 0.1mm to 5mm.

[0043] Furthermore, there are multiple separation net vertical parts 7, and multiple separation net vertical parts 7 are arranged around the inner wall of the reactor 1, and the heights of the multiple separation net vertical parts 7 are different. In addition, in some embodiments, the separation net vertical part 7 is provided with a cutting structure along its length direction, so as to cut the water body through the cutting structure. Specifically, the cutting structure is an irregular coiled steel wire arranged around the outside of the separation net vertical part 7, which can block and cut the water body.

[0044] In the first embodiment, the multi-channel fully mixed flow injection loop reaction device also includes a pressure detector 9 and a temperature detector 10. By detecting the pressure of the reactor 1 by the pressure detector 9 and the temperature detector 10 by detecting the temperature of the reactor 1, it is possible to better monitor the reaction process and ensure the normal progress of the reaction.

[0045] In addition, if Figure 6 As shown, in the second embodiment of the multi-channel full mixed flow injection loop reaction device of the present invention, the injection loop is a double loop, including two injectors 2 of different lengths and three liquid-liquid mixers 6, and three liquid-liquid mixing channels are connected to the three liquid-liquid mixers 6 respectively, so as to realize Figure 5 In addition, in the second embodiment, a pre-processor 11 and a pre-reaction circulation pump 12 are also included to achieve pre-reaction treatment of materials and improve reaction efficiency.

[0046] In addition, preferably, the liquid-liquid mixer 6 is detachably arranged in the reactor 1, so as to conveniently adjust the liquid-liquid mixer 6 to different heights, so as to better adapt to different reaction requirements. A reinforcement device may be provided between each corner of the gas-liquid separation network 5 and the cylinder of the reactor 1 to improve the stability of the gas-liquid separation network 5.

[0047] In addition, in some embodiments, in order to adapt to some relatively large-sized reactors, such as Figure 7-9 As shown, the injector 2 includes a first injection tube body 21 and a second injection tube body 22, wherein the first injection tube body 21 and the second injection tube body 22 are both in the shape of long strips, the length of the first injection tube body 21 is longer than the length of the second injection tube body 22, the bottom end of the first injection tube body 21 is located at the bottom end in the reactor 1, and the bottom end of the second injection tube body 22 is located at the top end in the reactor 1. Further, a first joint 211 is provided at the bottom end of the first injection tube body 21, and the first joint 211 is provided with a first injection pipe 212 and a second injection pipe 213, and a first delivery pipe connected to the injection circuit 31 is provided in the first injection tube body 21, and the first delivery pipe is respectively connected to the first injection pipe 212 and the second injection pipe 213, so as to deliver circulating liquid to the first injection pipe 212 and the second injection pipe 213 through the first delivery pipe.

[0048] Preferably, the bottom of the first injection pipe 21 is at a higher level than the top of the separation net vertical portion 7. It should be understood that the first injection pipe 21 is located at the center of the reactor 1, while the second injection pipe 22 is located on the side wall of the reactor 1.

[0049] Furthermore, the second injection pipe 213 is also connected to the first hose 214, and the first hose 214 is also connected to the first suspension ball 215, so that the circulating liquid of the second injection pipe 213 is transported to the first suspension ball 215 through the first hose 214, so as to output the circulating liquid from the first suspension ball 215. It should be understood that the first suspension ball 215 is suspended in the solution in the reactor 1, and will float and move to different positions, so that the circulating liquid sprayed from the first suspension ball 215 can be sprayed to different positions, the material is evenly distributed, and the material distribution uniformity and polymerization degree consistency are improved. That is to say, the position of the circulating liquid sprayed from the first injection pipe 212 is fixed, while the position of the circulating liquid output from the first suspension ball 215 is not fixed.

[0050] Specifically, the first suspension ball 215 includes a first suspension shell 2151, and a first receiving cavity 2152 and a second receiving cavity 2153 are provided in the first suspension shell 2151. The first receiving cavity 2152 and the second receiving cavity 2153 are sealed and not connected. Preferably, the second receiving cavity 2153 is provided in the first receiving cavity 2152.

[0051] The first receiving cavity 2152 is connected to the first hose 214, so that the circulating liquid in the first hose 214 is transported to the first receiving cavity 2152, so that the circulating liquid flows out of the first receiving cavity 2152. In addition, a second delivery pipe for delivering air is also provided in the first injection tube body 21, and the second delivery pipe is connected to the second receiving cavity 2153 of the first suspension shell 2151 through the second hose 216, so that air is delivered to the second receiving cavity 2153 through the second delivery pipe, so as to change the buoyancy of the first suspension ball 215, so that the first suspension ball 215 can be controlled to suspend at different positions in the solution as needed.

[0052] Specifically, when the buoyancy of the first suspension ball 215 needs to be increased, air is transported into the second receiving cavity 2153 through the second delivery pipe to increase the buoyancy of the first suspension ball 215; when the buoyancy of the first suspension ball 215 needs to be reduced, air is absorbed into the second receiving cavity 2153 through the second delivery pipe to absorb the gas in the first suspension ball 215, so that the buoyancy in the first suspension ball 215 becomes smaller. Furthermore, in the following special embodiment, a first position sensor for detecting the position of the first suspension ball 215 in the reactor 1 is further provided in the reactor 1. When the first position sensor detects that the position of the first suspension ball 215 in the reactor 1 is at the first preset position, the second conveying pipe is controlled to gradually convey air into the second receiving chamber 2153 to gradually increase the buoyancy of the first suspension ball 215, so that the first suspension ball 215 gradually rises. When the first position sensor detects that the position of the first suspension ball 215 in the reactor 1 is at the second preset position (wherein the second preset position is higher than the first preset position), the second conveying pipe is controlled to gradually absorb air into the second receiving chamber 2153 to gradually reduce the buoyancy of the first suspension ball 215, so that the first suspension ball 215 gradually descends, so that the first suspension ball 215 can be circulated up and down in the bottom of the reactor 1 to make the material evenly distributed.

[0053] Furthermore, a moving member 210 is movably provided outside the first spray tube 21 along its length direction, and the moving member is connected to the first suspension shell 2151 through the first pull rope 217 to limit the position of the first suspension ball 215 through the first pull rope 217, so that the first suspension ball 215 does not drift too far. It should be understood that although the solution in the reactor 1 has fluidity, in order to change the suspension position of the first suspension ball 215, it is still necessary to change the buoyancy of the first suspension ball 215 by changing the air in the first suspension ball 215 to achieve the change of the suspension position.

[0054] In addition, in some special embodiments, each of the plurality of separation net vertical parts 7 is coated with a first magnet layer of single magnetism, and the first suspension ball 215 is coated with a second magnet layer of single magnetism, wherein the first magnet layer and the second magnet layer have the same magnetism, so that when the first suspension ball 215 approaches the separation net vertical part 7, it will be repelled by the first magnet layer of the separation net vertical part 7 to move away from the separation net vertical part 7. Furthermore, the bottom end of the first injection tube body 21 is coated with a third magnet layer of single magnetism along its length direction, and the first magnet layer, the second magnet layer and the third magnet layer have the same magnetism, so that the first suspension ball 215 swings between the separation net vertical part 7 and the first injection tube body 21.

[0055] Furthermore, a second joint 221 is provided at the bottom end of the second injection tube body 22, and a third injection tube 222 and a fourth injection tube 223 are provided in the second joint 221. A third delivery pipe connected to the injection circuit 31 is provided in the second injection tube body 22, and the third delivery pipe is respectively connected to the third injection tube 222 and the fourth injection tube 223 to deliver circulating liquid to the third injection tube 222 and the fourth injection tube 223 through the third delivery pipe.

[0056] Furthermore, the fourth injection pipe 223 is also connected to the third hose 224, and the third hose 224 is also connected to the second suspension ball 225, so that the circulating liquid of the third hose 224 is transported to the second suspension ball 225 through the third hose 224, so as to output the circulating liquid from the second suspension ball 225. It should be understood that the second suspension ball 225 is suspended in the solution in the reactor 1, and will float and move to different positions, so that the circulating liquid sprayed from the second suspension ball 225 can be sprayed to different positions, the material is evenly distributed, and the material distribution uniformity and polymerization degree consistency are improved. That is to say, the position of the circulating liquid sprayed from the third injection pipe 222 is fixed, while the position of the circulating liquid output from the second suspension ball 225 is not fixed.

[0057] Specifically, the second suspension ball 225 includes a second suspension housing 2251, and a third receiving cavity 2252 and a fourth receiving cavity 2253 are provided in the second suspension housing 2251. The third receiving cavity 2252 and the fourth receiving cavity 2253 are sealed and not connected. Preferably, the fourth receiving cavity 2253 is provided in the third receiving cavity 2252.

[0058] The third receiving cavity 2252 is connected to the third hose 224, so that the circulating liquid in the third hose 224 is transported to the third receiving cavity 2252, so that the circulating liquid flows out of the third receiving cavity 2252. In addition, a fourth delivery pipe for delivering air is also provided in the second injection tube body 22, and the fourth delivery pipe is connected to the fourth receiving cavity 2253 of the second suspension shell 2251 through the fourth hose 226, so that air is delivered to the fourth receiving cavity 2253 through the fourth delivery pipe, so as to change the buoyancy of the second suspension ball 225, so that the second suspension ball 225 can be controlled to be suspended at different positions in the solution as needed.

[0059] Specifically, when the buoyancy of the second suspension ball 225 needs to be increased, air is transported into the fourth containing cavity 2253 through the fourth delivery pipe to increase the buoyancy of the second suspension ball 225; when the buoyancy of the second suspension ball 225 needs to be reduced, air is absorbed into the fourth containing cavity 2253 through the fourth delivery pipe to absorb the gas in the second suspension ball 225, so that the buoyancy in the second suspension ball 225 becomes smaller. Furthermore, in the following special embodiment, a second position sensor for detecting the position of the second suspension ball 225 in the reactor 1 is further provided in the reactor 1. When the second position sensor detects that the position of the second suspension ball 225 in the reactor 1 is at the third preset position, the fourth conveying pipe is controlled to gradually convey air into the fourth receiving chamber 2253 to gradually increase the buoyancy of the second suspension ball 225, so that the second suspension ball 225 gradually rises. When the second position sensor detects that the position of the second suspension ball 225 in the reactor 1 is at the fourth preset position (wherein the fourth preset position is higher than the first preset position, and the third preset position is higher than the second preset position), the fourth conveying pipe is controlled to gradually absorb air into the fourth receiving chamber 2253 to gradually reduce the buoyancy of the second suspension ball 225, so that the second suspension ball 225 gradually descends, so that the second suspension ball 225 can be circulated up and down in the bottom of the reactor 1 to make the material evenly distributed.

[0060] Compared with the prior art, the present invention provides a multi-channel fully mixed flow injection loop reaction device, which has the following beneficial effects: (1) The present invention adds multiple circulation channels (liquid-liquid mixing channels) to the injection loop, and adds multiple submerged mixing facilities (liquid-liquid mixers) on the basis of the original above-liquid gas-liquid reaction loop, so that the materials in the reactor are formed into a fully mixed flow form, and the continuous phase materials and dispersed phase materials in the reactor are evenly distributed. Each node in the reactor has the same reaction probability, which improves the uniformity of material distribution and the consistency of polymerization degree, and achieves the consistency of the material circulation period in the reactor; (2) The reactor of the present invention adds a rapid separation device (gas-liquid separation network) for separating gas from liquid, which can The non-reactive gases such as N2 carried by the ejector are efficiently and quickly separated from the liquid material to enter the upper gas phase space of the reactor, thereby avoiding the rapid decline in the capacity of the reactor heat exchange system or even paralysis, which may cause the decline in production efficiency and potential safety hazards; (3) The original reaction kinetic energy is driven by the pump kinetic energy, but after the present invention adds a submerged circuit, the pump kinetic energy mainly realizes the mixing of the gas-liquid phase (dispersed phase and continuous phase), and the liquid-liquid mixer further provides reaction kinetic energy. The driving force required for liquid-liquid mixing is much lower than that for gas-liquid driving, which doubles the effect and realizes reactor consumption reduction and efficiency improvement; (4) The present invention is provided with a submerged mixer (liquid-liquid mixer), which only requires a flow rate of 1-5 times the volume of the reaction material (i.e., 1m 3 The material needs 1~5m 3 / h circulation flow rate) can achieve the uniformity of the continuous phase and the dispersed phase in the reactor, improve the reaction efficiency and achieve the consistency of polymerization degree; (5) Compared with the original process, the present invention can use a single-loop reactor when the double circulation is not required for the formula growth ratio, and there is no problem of inconsistent product polymerization degree, which reduces equipment investment, reduces operating costs and improves product quality; (6) In the original injection loop process, about 50% to 80% of the dispersed phase reacts in the ejector in each cycle, and the material after entering the reactor through the ejector outlet is basically close to the plug flow reaction. There is a risk of explosion at high dispersed phase concentrations, and there are no reaction conditions at low dispersed phase concentrations, and the quality and efficiency are insufficient; the present invention Through the action of the liquid-liquid mixer, the materials in the reactor are nearly fully mixed in a uniform phase, which accelerates the reaction efficiency and eliminates the risk of explosion. The dispersed phase reaction ratio can reach 70% to 95% in each cycle; (7) The gas-liquid separation network of the present invention can quickly separate the inert gas such as nitrogen entrained by the ejector, so that the gas phase ratio of the materials in the reactor decreases when they enter the cycle again. When the product viscosity is lower than 200cp, the heat exchange efficiency of the heat exchanger is basically not affected, and the process is safe to operate. The process is adapted to increase the product viscosity from 50cp to 200cp. It can be understood that the present invention can enable the reactor to quickly achieve gas-liquid separation and improve the mass transfer efficiency by setting a liquid-liquid mixer and a gas-liquid separation network.

[0061] It should be noted that the terms "include", "comprises" or any other variations thereof are intended to cover non-exclusive inclusion, so that a process, method, article or device including a series of elements includes not only those elements, but also other elements not explicitly listed, or also includes elements inherent to such process, method, article or device. In the absence of further restrictions, an element defined by the sentence "comprises a ..." does not exclude the existence of other identical elements in the process, method, article or device including the element.

[0062] Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that various changes, modifications, substitutions and variations may be made to the embodiments without departing from the principles and spirit of the present invention, and that the scope of the present invention is defined by the appended claims and their equivalents.

Claims

1. A multi-channel fully mixed flow jet loop reaction device, comprising a reactor, an ejector and an ejection loop, wherein the ejector is arranged at the top of the cylinder of the reactor, the ejection loop connects the feed port of the ejector and the discharge port of the reactor, and the ejection loop is provided with a reaction circulation pump, characterized in that: The multi-channel fully mixed flow injection loop reaction device also includes a gas-liquid separation network and a plurality of liquid-liquid mixers. The plurality of liquid-liquid mixers are distributed in the reactor at different heights below the liquid of the reactor. The injection loop is connected to a plurality of liquid-liquid mixing channels to be correspondingly connected to each of the liquid-liquid mixers. The gas-liquid separation network is arranged in the reactor and close to the bottom of the reactor cylinder.

2. The multi-channel fully mixed flow jet loop reaction device according to claim 1, characterized in that: The injection circuit is a single circuit or multiple circuits.

3. The multi-channel fully mixed flow injection loop reaction device according to claim 2, characterized in that: When the injection circuit is a multi-circuit circuit, a plurality of the liquid-liquid mixing channels are connected to any circuit or multiple circuits of the injection circuit.

4. The multi-channel fully mixed flow injection loop reaction device according to claim 1, characterized in that: The plurality of liquid-liquid mixers adopt one or a combination of a rotating nozzle, a multi-channel multi-directional nozzle, and the ejector.

5. The multi-channel fully mixed flow jet loop reaction device according to claim 1, characterized in that: The surface of the gas-liquid separation net is made of hydrophobic material or coated with a hydrophobic coating.

6. The multi-channel fully mixed flow jet loop reaction device according to claim 1, characterized in that: The gas-liquid separation net comprises a separation net vertical portion and a separation net bottom. The separation net vertical portion is arranged close to the cylinder side wall of the reactor, and the separation net bottom is arranged close to the cylinder bottom of the reactor.

7. The multi-channel fully mixed flow jet loop reaction device according to claim 6, characterized in that: The mesh diameter of the vertical part of the separation net is 1 μm to 800 μm, and the mesh diameter of the bottom of the separation net is 0.1 mm to 5 mm.

8. The multi-channel fully mixed flow jet loop reaction device according to claim 6, characterized in that: The bottom of the separation net is in an inverted arc shape or a downward cone shape.

9. The multi-channel fully mixed flow jet loop reaction device according to claim 1, characterized in that: The gas-liquid separation network adopts a non-flat structure, and the injection loop is also provided with a circulating heat exchanger.

10. The multi-channel fully mixed flow jet loop reaction device according to claim 1, characterized in that: The injector includes a first injection tube body and a second injection tube body, wherein the first injection tube body and the second injection tube body are both in the shape of long strips, the length of the first injection tube body is longer than the length of the second injection tube body, the bottom end of the first injection tube body is at the bottom end in the reactor, and the bottom end of the second injection tube body is at the top end in the reactor.

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