Multiphase unpowered reactor

Abstract

The utility model belongs to the technical field of reactors, and particularly relates to a multiphase unpowered reactor, which comprises a vertical shell, an upper reaction area and a lower liquid collection area are arranged in the shell, and the reaction area is communicated with the liquid collection area through a cap hood, and is characterized in that an annular pipe is arranged in the middle of the reaction area and is connected with a feed port of the shell through a feed pipe; a plurality of horizontal circulating hydraulic sprayers are arranged on the annular pipe, and the axis of at least one horizontal circulating hydraulic sprayer is tangential to the outer side of the annular pipe; a cross pipe is arranged at the lower part of the reaction area; a plurality of vertical circulating hydraulic sprayers are arranged on the cross pipe; and the horizontal circulating hydraulic spray head and the vertical circulating hydraulic spray head are venturi mixed flow spray heads. The utility model has the beneficial effects that the middle section and the lower section of the reaction area of the shell adopt two sections of liquid-phase hydraulic sprayers to be combined with the atomizing sprayers at the top of the reaction area to respectively form liquid flow in the vertical direction and the horizontal direction, so that the mixing effect of gas-phase, liquid-phase and solid-phase substances is enhanced, and the conversion efficiency is improved.

Description

TECHNICAL FIELD

[0001] The utility model belongs to the technical field of reactor, especially relate to a multiphase state unpowered reactor. BACKGROUND

[0002] At present, the ethoxylation reaction is carried out in an ethoxylation reactor, and the structural form of the ethoxylation reactor mainly includes three types of agitated ethoxylation reactor, PRESS ethoxylation reactor and BUSS ethoxylation reactor. In order to improve the safety and stability of the reaction process, it is necessary to have strong stirring capacity, wherein:

[0003] 1. The agitated ethoxylation reactor is used for the ethoxylation reaction. Ethylene oxide enters from the distributor at the bottom of the reactor, and under the action of the agitator, the ethylene oxide is reacted with the starting agent liquid phase in the form of dispersion, vaporization and bubbling. The unreacted ethylene oxide enters the top of the reactor, and continues to react on the surface of the liquid level of the reactor. The gas-liquid contact surface of this type of reactor is small, and the dispersion performance of the gas is poor, so as to affect the molecular weight distribution and product quality. The biggest disadvantage is that the moving parts of the agitator are exposed to the gas phase of ethylene oxide, which is easy to leak and generate static electricity due to friction, and there is a safety hazard.

[0004] 2. The PRESS ethoxylation reactor is used for the ethoxylation reaction. The material is mixed with ethylene oxide in the form of spray, so that the gas phase of ethylene oxide and the liquid phase of the circulating material are dispersedly contacted in the maximum limit, and part of the ethylene oxide is dissolved in the material to react. Here, ethylene oxide is the continuous phase, and the reaction material is the dispersed phase. The PRESS ethoxylation reactor is a loop reactor, which uses an external circulation heat exchanger to remove the reaction heat, and the reaction rate is much higher than that of the agitated reactor.

[0005] 3. The BUSS ethoxylation reactor is used for the ethoxylation reaction. The principle of the Venturi jet mixer is used to mix and react the gas phase of ethylene oxide and the circulating material. That is, the local low pressure area at the throat is caused by the jet of the material, and the ethylene oxide gas is sucked into the Venturi mixer. Here, the material is the continuous phase, and the ethylene oxide is the dispersed phase. The dispersion performance of ethylene oxide in the Venturi mixer is good, so the reaction rate is high.

[0006] Xu Zhiyang of China International Engineering Corporation published a paper "Process Review of Ethoxylation Device", which introduces the ethoxylation production process, and compares and analyzes the process, equipment and automatic control of the ethoxylation device currently used in China. The combined ethoxylation process is introduced, which is summarized as follows:

[0007] (1) Ethoxylation process combined with stirring and spraying (see Figure 8) is a kind of ethoxylation reactor which is derived from stirred tank reactor, and the reactor is added with circulating spray mixer on the basis of original stirred reactor, so as to increase gas-liquid contact surface, improve reaction rate and product quality.

[0008] (2) Ethoxylation process combined with stirrer and venturi mixer (see Figure 9 ) is a kind of ethoxylation device combined with stirrer and venturi mixing reactor, which is developed by using the advantages of venturi mixer and the characteristics of stirred reactor, and the reactor can adapt to reaction process with great viscosity variation and can be used in production of high-viscosity products.

[0009] (3) Ethoxylation process combined with spray mixer and venturi mixer (see Figure 10 ) is a kind of ethoxylation reactor which is based on spray mixing reactor and absorbs the advantages of venturi mixer of BUSS process. The reactor is added with venturi mixer in the outer circulation loop, so that the unreacted ethylene oxide in the head space of the reactor can also be absorbed into the material to participate in the reaction, thereby shortening the reaction maturation stage time and reducing the content of E0 in the product and exhaust tail gas.

[0010] (4) Ethoxylation process combined with venturi and spray (see Figure 11 ) is a kind of ethoxylation reactor which is based on spray mixing reactor and absorbs the advantages of venturi mixer of BUSS process. The reactor is added with venturi mixer in the outer circulation loop, so that the unreacted ethylene oxide in the head space of the reactor can also be absorbed into the material to participate in the reaction, thereby shortening the reaction maturation stage time and reducing the content of E0 in the product and exhaust tail gas.

[0011] It can be seen that it is an eternal development topic in the industry to continuously optimize the internal structure of ethoxylation reactor to make it more conducive to improving reaction efficiency and making the mixing of gas phase, liquid phase or gas phase, liquid phase and solid phase more sufficient. Practical new type content

[0012] The utility model aims at providing a kind of multiphase state unpowered reactor, overcome the deficiency of prior art, adopt two-stage liquid phase hydraulic jet in the middle section and lower section of the reaction zone of shell and combine with atomizing nozzle in the top of reaction zone, liquid flow that hydraulic jet sprays pushes the liquid phase and solid phase in the bottom of reaction zone to flow upwards, respectively form liquid flow in vertical direction and horizontal direction, enhance the mixing effect of gas phase, liquid phase and solid phase material, improve the conversion efficiency of gas phase alkyl alkane.

[0013] To achieve the above object, the utility model realizes by following technical scheme:

[0014] A multi-phase state non-powered reactor comprises a vertical shell, a reaction zone at the upper part and a liquid collecting zone at the lower part in the shell, a cap cover is arranged at the joint of the reaction zone and the liquid collecting zone, the reaction zone and the liquid collecting zone are communicated through the cap cover, a ring pipe is arranged at the middle part of the reaction zone, the ring pipe is connected with a feeding port on the top head of the shell through a feeding pipe, a plurality of horizontal circulating hydraulic nozzles are arranged on the ring pipe, and the axis of at least one horizontal circulating hydraulic nozzle is tangentially arranged outside the ring pipe; a cross pipe is arranged at the lower part of the reaction zone, a plurality of vertical circulating hydraulic nozzles are arranged on the cross pipe, the axis of at least one vertical circulating hydraulic nozzle is arranged at a downward 75-85° angle A1 with the cross pipe, the axis of at least one vertical circulating hydraulic nozzle is arranged at a upward 55-75° angle A2 with the cross pipe and at a outward 18-22° angle A3 with the cross pipe, the axis of at least one vertical circulating hydraulic nozzle is arranged at a upward 35-45° angle A4 with the cross pipe and at a inward 40-50° angle A5 with the cross pipe; the horizontal circulating hydraulic nozzle and the vertical circulating hydraulic nozzle are both Venturi mixed flow nozzles.

[0015] Further, the bottom of the liquid collecting zone is connected with a mother liquor circulating pipe.

[0016] Further, the top of the cap cover is connected with the cross pipe through a support.

[0017] Further, the cap cover comprises a top cap and a cover cylinder, the top cap is connected with the cover cylinder through a connecting rod, the lower side of the top cap and the upper side of the cover cylinder form a liquid flowing channel, the surface of the cover cylinder is provided with an outward convex bending belt, and the bottom of the cover cylinder is provided with an outflow hole.

[0018] Further, the top of the reaction zone is provided with an atomizing nozzle, the atomizing nozzle is arranged on a linear and / or annular spray pipe, the linear spray pipe is arranged at the top of the reaction zone, and the annular spray pipe is arranged on the side wall of the gas (vapor) phase space of the reaction zone; the atomizing nozzle is any one of a solid cone circular nozzle, a hollow cone circular atomizing nozzle and a fan-shaped straight-line nozzle.

[0019] Further, at least one of the vertical circulating hydraulic nozzles is a rotating water jet nozzle capable of cleaning the bottom of the reaction zone.

[0020] Further, the atomizing nozzle is connected with a first mother liquor feeding pipe, one end of the cross pipe is connected with a second mother liquor feeding pipe, and the other three ends are blocked.

[0021] Further, the feeding port is connected with the outlet end of a Venturi mixer through a pipeline.

[0022] Further, the vertical circulating hydraulic nozzles are arranged in a concentric circle direction on the cross pipe, and the outlet directions of the nozzles on the same circle are consistent in rotation direction.

[0023] Further, the ring pipe is composed of multiple segments, and each segment is connected through quick flanges; the outlet directions of the horizontal circulating water spray heads on the ring pipe are consistent in rotation.

[0024] Compared with the prior art, the utility model has the advantages of:

[0025] 1) Two-stage liquid-phase water spray heads are used in the middle section and the lower section of the shell reaction zone, and are combined with the atomizing spray head at the top of the reaction zone, the liquid flow sprayed by the water spray heads drives the liquid phase and the solid phase at the bottom of the shell reaction zone to flow upwards, respectively forming liquid flow in the vertical direction and the horizontal direction, enhancing the mixing effect of the gas phase, the liquid phase and the solid phase, and improving the conversion efficiency of the gas phase alkylene oxide.

[0026] 2) The reactor feed port is connected with a Venturi mixer, the Venturi mixer is provided with gas-phase and liquid-phase connecting ports, which is beneficial to enhancing the mixing efficiency of the gas phase and the liquid phase, the gas phase is connected to the low-pressure area of the jet mixer, and the system pressure is low.

[0027] 3) The atomizing spray head at the top of the reaction zone can capture unreacted alkylene oxide droplets, and reduce the alkylene oxide content in the tail gas.

[0028] 4) The two-stage liquid-phase water spray heads can effectively control the reaction temperature in the reactor, avoid that the system temperature is too high or too low (resulting in accumulation of alkylene oxide), and more effectively control the temperature and pressure parameters of the system.

[0029] 5) The utility model can be applied to the reaction processes of various gas / liquid, liquid / liquid and gas / liquid / solid systems. BRIEF DESCRIPTION OF DRAWINGS

[0030] Figure 1 is a schematic diagram of the internal structure of the utility model embodiment;

[0031] Figure 2 is a schematic diagram of the ethoxylation reaction system of the utility model embodiment;

[0032] Figure 3 is a schematic diagram of the ring pipe structure in the utility model embodiment;

[0033] Figure 4 is a schematic diagram of the cross pipe structure in the utility model embodiment; Figure 3

[0034] Figure 5 is a schematic diagram of the cross pipe structure in the utility model embodiment;

[0035] Figure 6 is a top view of Figure 5

[0036] Figure 7 ​​Is the cap structure schematic diagram of the embodiment of the utility model;

[0037] Figure 8 Is the existing technology in the stirring and spraying combination of ethoxylation process flow chart;

[0038] Figure 9 Is the existing technology in the stirrer and venturi mixer combination of ethoxylation process flow chart;

[0039] Figure 10 Is the existing technology in the spray mixer and venturi mixer combination of ethoxylation process flow chart;

[0040] Figure 11 Is the existing technology in the venturi and spray combination of ethoxylation process flow chart;

[0041] In the drawing: 1-reaction zone, 2-liquid collection area, 3-cap, 4-ring tube, 5-feeding pipe, 6-feeding port, 7-horizontal circulating hydraulic nozzle, 8-cross pipe, 9-vertical circulating hydraulic nozzle, 10-bracket, 11-outflow hole, 12-atomizing nozzle, 13-first mother liquor inlet pipe, 14-second mother liquor inlet pipe, 15-venturi mixer, 16-quick flange, 17-tail gas port, 18-mother liquor circulating pipe, 19-cleaning manhole, 20-ring-shaped spray pipe, 21-top cap, 22-cylinder cover, 23-connecting rod, 24-bent belt, 25-mother liquor main pipe. DETAILED DESCRIPTION

[0042] The technical scheme of the utility model will be described clearly and completely in combination with specific embodiments, obviously, the described embodiments are a part of the embodiments of the utility model, not all the embodiments.

[0043] In order to more clearly illustrate the specific embodiment of the utility model or the technical scheme in the prior art, the specific embodiments needed in the specific embodiment or prior art description will be briefly introduced, obviously, the specific embodiments in the following description are some embodiments of the utility model, and for those skilled in the art, other specific embodiments can be obtained without creative labor.

[0044] The components of the embodiments of the utility model described and shown in the specific embodiments here can be arranged and designed in countless different configurations. Therefore, the following detailed description of the embodiments of the utility model provided in the specific embodiments is not intended to limit the scope of the claimed utility model, but only represents selected embodiments of the utility model.

[0045] See Figures 1-7The utility model discloses a multi-phase state unpowered reactor structure schematic diagram, including vertical casing, the casing top is equipped with tail gas port 17, and the lateral wall of casing is equipped with the clearance manhole 19 of cleaning, is equipped with the reaction area 1 of upper portion and lower portion's liquid collection area 2 in the casing, and the bottom of liquid collection area 2 is connected mother liquor circulation pipe 18, and after heating or heat removal through heat exchanger, return feed inlet 6, the connecting place of reaction area 1 and liquid collection area 2 is equipped with cap 3, and reaction area 1 and liquid collection area 2 are connected through cap 3, and the middle part of reaction area 1 is equipped with ring pipe 4, and ring pipe 4 is connected with the feed inlet 6 on the top head of casing through feed pipe 5, and feed inlet 6 is connected with the outlet end of venturi mixer 15 by pipeline. The utility model embodiment can realize the gas (vapor) / liquid system reaction, gas (vapor) / liquid / solid system reaction, liquid / solid system reaction process based on homogeneous and heterogeneous catalytic system.

[0046] The utility model embodiment improves the heat transfer and mass transfer efficiency by optimizing the hydraulic stirring design, realizes the "unpowered" hydraulic stirring instead of the traditional stirrer, cancels the traditional mechanical seal component, and greatly improves the safety of the reaction system and the reliability of the equipment. The venturi mixer is arranged at the reactor feed, and the raw materials and raw material-catalyst configuration liquid are introduced into the system through the low-pressure side of the venturi mixer by using the circulating mother liquor power, and the raw materials and raw material-catalyst configuration liquid can be uniformly mixed.

[0047] A plurality of horizontal circulating hydraulic nozzles 7 are arranged on the ring pipe 4, and the axis of at least one horizontal circulating hydraulic nozzle 7 is tangentially arranged outside the ring pipe 4. The ring pipe 4 is composed of multiple segments, and the segments are connected through quick flanges 16. The outlet directions of the horizontal circulating hydraulic nozzles 7 on the ring pipe 4 are consistent.

[0048] A plurality of vertical circulating hydraulic nozzles 9 are arranged on the cross pipe 8, and the axis of at least one vertical circulating hydraulic nozzle 9 forms a downward inclination angle A1 of 75-85° with the cross pipe 8. The axis of at least one vertical circulating hydraulic nozzle 9 forms an upward inclination angle A2 of 55-75° with the cross pipe 8 and an outward inclination angle A3 of 18-22° with the cross pipe 8. The axis of at least one vertical circulating hydraulic nozzle 9 forms an upward inclination angle A4 of 35-45° with the cross pipe 8 and an inward inclination angle A5 of 40-50° with the cross pipe 8. The vertical circulating hydraulic nozzles 9 are arranged in a concentric circle direction on the cross pipe 8, the outlet directions of the nozzles on the same circle are consistent, and a vertical stirring zone is formed. In the embodiment, the horizontal circulating hydraulic nozzles 7 and the vertical circulating hydraulic nozzles 9 are venturi mixed flow nozzles, and the venturi mixed flow nozzles are in a threaded installation form. In the embodiment, the inclination angle values are preferably A1 of 80°, A2 of 60°, A3 of 20°, A4 of 42°, and A5 of 45°.

[0049] The atomizing nozzle 12 is arranged in the gas phase space in the reaction zone, so that the mother liquor forms fine liquid droplets, the contact efficiency between the mother liquor and the gas phase is improved, and the reaction efficiency is improved, the raw material conversion rate is improved, and the system pressure accumulation is avoided. The hydraulic nozzle on the cross pipe 8 and the cross pipe 8 can further strengthen the mass transfer and heat transfer of the reaction material. Through the above process, efficient reaction in the gas phase space and the liquid phase space in the reactor can be realized.

[0050] The top of the cap 3 is connected with the cross pipe 8 through the support 10. The cap 3 includes a top cap 21 and a cover cylinder 22, and the top cap 21 is connected with the cover cylinder 22 through a connecting rod 23. The lower side of the top cap 21 and the upper side of the cover cylinder 22 form a liquid flow channel. The surface of the cover cylinder 22 is provided with an outwardly convex bending belt 24. The bottom of the cover cylinder 22 is provided with a flow-out hole 11. The flow-out hole 11 is used to make the mother liquor quickly enter the reactor from the bottom before the reaction starts, and to minimize the solid material entering the liquid collection area during the reaction. The cap 3 can effectively avoid the solid material falling into the liquid collection area 2 and blocking the bottom outlet during the solid material feeding process. The cap 3 is matched with the vertical circulating hydraulic nozzle 9 to make the solid material fully suspended in the liquid phase.

[0051] The top of the reaction zone 1 is provided with an atomizing nozzle 12. The atomizing nozzle is arranged on a linear and / or annular spray pipe. The linear spray pipe is arranged at the top of the reaction zone, and the annular spray pipe 20 is arranged on the side wall of the gas phase space of the reaction zone. The atomizing nozzle 12 is any one of a solid cone-shaped nozzle, a hollow cone-shaped atomizing nozzle 12, and a fan-shaped straight-line nozzle. The atomizing nozzle 12 is connected with a first mother liquor inlet pipe 13. One end of the cross pipe 8 is connected with a second mother liquor inlet pipe 14, and the other three ends are blocked. The annular spray pipe 20 is connected with a mother liquor main pipe 25 through a pipeline.

[0052] In order to reduce the deposition of solid phase material at the bottom of the reaction zone, at least one vertical circulating hydraulic nozzle 9 is a rotating water jet nozzle which can clean the bottom of the reaction zone 1.

[0053] In the gas phase space at the upper part of the reaction zone, the reaction process is that the liquid phase droplets are uniformly dispersed in the gas phase, cover the dead angle of the gas phase space, realize the capture of the gas, and the fine liquid droplets fully react with the escaped gas material in the gas phase space, so as to improve the reaction efficiency.

[0054] In the liquid phase space in the middle part of the reaction zone, after the preliminary mixing of the Venturi mixer, the raw materials participating in the reaction are dispersed into the liquid phase again by the horizontal circulating hydraulic nozzle through the outlet residual pressure of the Venturi mixer 15, and the horizontal direction rotation trend of the middle part of the reaction zone is realized by the hydraulic stirring, so as to further improve the reaction efficiency of the gas phase space.

[0055] In the liquid phase space in the lower part of the reaction zone, the upper and lower direction trend hydraulic stirring is formed by the cross pipe 8 and the vertical circulating hydraulic jet 9, and the lower raw material is continuously pushed upward to the middle section to contact and react with the raw material, and meanwhile, the vertical direction force is formed with the middle horizontal stirring zone to strengthen the overall disturbance. The vertical circulating hydraulic jet 9 on the cross pipe 8 is arranged in a polar coordinate symmetry mode, and the vertical direction (i.e. the axial direction of the reactor) hydraulic stirring is formed. For the solid phase reaction system, the double-layer disturbance formed by the utility model can avoid the solid deposition, and the solid can be fully dispersed into the liquid phase space, and the reaction efficiency is improved.

[0056] See Figure 2 In the ethoxylation reaction system schematic diagram of the utility model embodiment, the reaction process is as follows: the raw material A feeding stage, the raw material A is added into the reactor according to the reaction ratio first, so that the system can establish liquid phase circulation, the mother liquor circulating pump is started, and the heat exchanger on the external circulating pipeline is passed, so that the system is preheated in the initial stage, and the system reaches the reaction initiation temperature.

[0057] The catalyst C feeding stage utilizes the venturi mixer 15 to bring the catalyst C into the reaction system, and the catalyst C can be added into the reactor in one-time pre-addition mode, or can be added according to a certain proportion according to the ratio of the raw material A / B in the reaction process, or can be added in different amounts in batches according to different reaction stages, or can be added in different catalysts according to different reaction stages and product requirements and the like.

[0058] The raw material B feeding reaction stage, after the system temperature and the catalyst amount meet the reaction conditions, the raw material B control valve is started, and the raw material is mixed F2 stream after passing through the venturi mixer and then enters the reactor. Through the ring pipe 4, the raw material is uniformly dispersed into the reactor, and the horizontal direction hydraulic stirring is formed, and if B is a gas raw material, the horizontal circulating hydraulic jet 7 is uniformly released into the liquid phase.

[0059] After the raw material B enters the reactor, due to the pressure reduction, the raw material B is rapidly released, and the micro-bubbles are formed, and the mass transfer and heat transfer are strengthened, and due to the property of the raw material B, the unreacted material escapes into the gas phase space, and the circulating mother liquor is atomized into small liquid by the atomizing jet 12 to capture the reactants in the gas phase.

[0060] The vertical circulating hydraulic jet 9 at the bottom of the reaction zone disturbs and strengthens the reaction efficiency of the raw material in the liquid phase, and strengthens the mass transfer and heat transfer, and if the system contains solid, the solid can be fully suspended in the vertical stirring zone under the vertical stirring force. The maximum allowable solid content in the system liquid phase is about 50%.

[0061] In the external circulation heat removal process, the reaction system material is taken out from the bottom outlet of the liquid collecting area 2 by the mother liquor circulating pump, and is removed by the heat exchange medium of the heat exchanger, and meanwhile, precise temperature control can be realized by bypass or setting external circulation heat exchangers with different heat loads, and effective temperature control is the basic guarantee for reaction safety.

[0062] The low-pressure area of the Venturi mixer 15 is provided with two feed inlets, according to the system, the reactor gas phase control valve can be opened in the reaction process or at the end of the reaction, and the gas-liquid contact and mass transfer process are strengthened by using the Venturi mixer 15.

[0063] At the end of the reaction, the raw material feed valve is closed, the gas (vapor) phase pipe opening is opened, the low gas pressure formed at the throat diameter of the Venturi mixer 15 makes the gas (vapor) phase material accelerate to dissolve into the liquid phase material, and the reaction is further promoted, when the gas (vapor) pressure in the reactor is stable, it indicates that the raw material in the gas (vapor) is completely reacted and consumed, the utility model improves the reaction conversion rate, reduces the material consumption, and also reduces the tail gas emission.

[0064] Although the embodiments of the utility model have been shown and described, it can be understood by those skilled in the art that various changes, modifications, replacements and variations can be made to these embodiments without departing from the principles and spirits of the utility model, and the scope of the utility model is defined by the appended claims and their equivalents.

Claims

1. A multi-phase state non-powered reactor comprising a vertical shell, a reaction zone in the upper part of the shell and a liquid collecting zone in the lower part of the shell, a cap cover is arranged at the joint of the reaction zone and the liquid collecting zone, the reaction zone and the liquid collecting zone are communicated through the cap cover, characterized in that, The middle part of the reaction zone is provided with a ring pipe connected with the feed inlet on the top head of the shell through a feed pipe, and a plurality of horizontal circulating hydraulic nozzles are arranged on the ring pipe, and the axis of at least one horizontal circulating hydraulic nozzle is tangentially arranged outside the ring pipe.

2. A multiphase state non-powered reactor according to claim 1, characterized in that, The bottom of the liquid collecting zone is connected with a mother liquor circulating pipe.

3. A multiphase state non-powered reactor according to claim 1, characterized in that, The top of the cap is connected with the cross pipe through a support.

4. A multiphase state non-powered reactor according to claim 1 or 2, characterised in that, The cap comprises a top cap and a cover cylinder, the top cap and the cover cylinder are connected through a connecting rod, the lower side of the top cap and the upper edge of the cover cylinder are connected through a channel for liquid phase flow, the surface of the cover cylinder is provided with an outward convex bending belt, and the bottom of the cover cylinder is provided with an outflow hole.

5. A multiphase state non-powered reactor according to claim 1, characterized in that, The top of the reaction zone is provided with an atomizing nozzle, the atomizing nozzle is arranged on a linear and / or annular spray pipe, the linear spray pipe is arranged at the top of the reaction zone, and the annular spray pipe is arranged on the side wall of the vapor phase space of the reaction zone; the atomizing nozzle is any one of a solid cone circular nozzle, a hollow cone circular atomizing nozzle and a fan-shaped straight-line nozzle.

6. A multiphase state non-powered reactor according to claim 1, characterized in that, At least one of the vertical circulating hydraulic nozzles is a rotating water jet nozzle capable of cleaning the bottom of the reaction zone.

7. A multiphase state unpowered reactor according to claim 5, wherein, The atomizing nozzle is connected with a first mother liquor inlet pipe, one end of the cross pipe is connected with a second mother liquor inlet pipe, and the other three ends are blocked.

8. A multiphase state non-powered reactor according to claim 1, characterized in that, The feed inlet is connected with the outlet end of the Venturi mixer through a pipeline.

9. A multiphase state non-powered reactor according to claim 1, characterized in that, The vertical circulating hydraulic nozzles are arranged in a concentric circle direction on the cross pipe, and the outlet directions of the nozzles on the same circle are consistent.

10. A multiphase state unpowered reactor according to claim 1, wherein, The ring pipe is composed of multiple segments, and the segments are connected through quick flanges; the outlet directions of the horizontal circulating hydraulic nozzles on the ring pipe are consistent.

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