阅读说明：本技术 提高丙烯水合反应效果的反应器 (Reactor for improving hydration reaction effect of propylene ) 是由 张绍志 陈金玉 周永美 赵建标 申林 王卫明 吴建仲 舒晨 王许宗 杨梵 于 2021-06-30 设计创作，主要内容包括：本发明公开了一种提高丙烯水合反应效果的反应器,反应器内固定连接有催化剂隔层A,催化剂隔层A将反应器内分隔成混合区A和逸出区,催化剂隔层A包括环形催化剂隔层和中心催化剂隔层,反应器的内侧壁、对应位于环形催化剂隔层顶面固定有微界面发生器,微界面发生器包括多个微界面发生器单元,微界面发生器单元均通过丙烯进气支管与丙烯供气装置连通,反应器侧壁、位于混合区A内分别连通有多个纯水进液支管,进液方向为切线方向,纯水进液支管与纯水供水装置连通,反应器顶部设有出气管。从上述结构可知,本发明的提高丙烯水合反应效果的反应器,提高了丙烯水合反应的效果,提高了异丙醇的得率。(The invention discloses a reactor for improving the hydration reaction effect of propylene, wherein a catalyst interlayer A is fixedly connected in the reactor, the catalyst interlayer A divides the interior of the reactor into a mixing area A and an escape area, the catalyst interlayer A comprises an annular catalyst interlayer and a central catalyst interlayer, a micro-interface generator is fixed on the inner side wall of the reactor and correspondingly positioned on the top surface of the annular catalyst interlayer, the micro-interface generator comprises a plurality of micro-interface generator units, the micro-interface generator units are communicated with a propylene gas supply device through propylene gas inlet branch pipes, a plurality of pure water liquid inlet branch pipes are respectively communicated with the side wall of the reactor and positioned in the mixing area A, the liquid inlet direction is tangential, the pure water inlet branch pipes are communicated with a pure water supply device, and an air outlet pipe is arranged at the top of the reactor. According to the structure, the reactor for improving the propylene hydration reaction effect improves the propylene hydration reaction effect and improves the yield of the isopropanol.)

1. Improve reactor of propylene hydration reaction effect which characterized in that: including reactor (1), fixedly connected with catalyst interlayer A (2) in reactor (1), catalyst interlayer A (2) separate the mixed zone A (3) that is located catalyst interlayer A (2) below and escape zone (4) that are located catalyst interlayer A (2) top with separating in reactor (1), catalyst interlayer A (2) are including annular catalyst interlayer (16) that are fixed in reactor (1) inside wall and central catalyst interlayer (17) that are fixed in annular catalyst interlayer (16) inboard through closing plate A (15), through closing plate A (15) seal partition between annular catalyst interlayer (16) and central catalyst interlayer (17), the inside wall of reactor (1), correspond fixedly connected with micro-interface generator that is located annular catalyst interlayer (16) top surface, micro-interface generator includes a plurality of micro-interface generators along annular catalyst interlayer (16) evenly distributed in proper order The reactor comprises a reactor unit (5), wherein the micro-interface generator unit (5) is sequentially spliced and forms an annular structure matched with an annular catalyst interlayer (16), each micro-interface generator unit (5) is respectively communicated with a propylene gas supply device through a propylene gas inlet branch pipe (6) penetrating through the side wall of the reactor (1), the top surface of each micro-interface generator unit (5), one side end surface facing the axis of the reactor (1) and a sealing plate B (18) fixedly connected with the end surfaces between two adjacent micro-interface generator units (5) are respectively communicated with a plurality of pure water liquid inlet branch pipes (7), the pure water inlet branch pipes (7) are uniformly distributed by taking the axis of the reactor (1) as the center, and the liquid inlet direction of each pure water inlet branch pipe (7) into the reactor (1) is the tangential direction of the corresponding position of the reactor (1), the water inlet angular velocity direction when entering the reactor (1) through the pure water liquid inlet branch pipe (7) is the same, the pure water liquid inlet branch pipe (7) is communicated with the pure water supply device respectively, and the top of the reactor (1) is also provided with an air outlet pipe (8).

2. The reactor for improving the hydration reaction of propylene according to claim 1, wherein: the reactor is characterized in that a catalyst interlayer B (2 ') is fixedly connected to the reactor (1) and positioned below the catalyst interlayer A (2), the catalyst interlayer B (2') separates a mixing region A (3) in the reactor (1) into a mixing region B (3 ') positioned between the catalyst interlayer A (2) and the catalyst interlayer B (2'), the catalyst interlayer B (2 ') has the same structure as the catalyst interlayer A (2), and also comprises an annular catalyst interlayer (16) fixed on the inner side wall of the reactor (1) and a central catalyst interlayer (17) fixed on the inner side of the annular catalyst interlayer (16) through a sealing plate A (15), the annular catalyst interlayer (16) and the central catalyst interlayer (17) are sealed and separated through the sealing plate A (15), and the inner side wall of the reactor (1) and the top surface of the annular catalyst interlayer (16) correspondingly positioned on the catalyst interlayer B (2') are also correspondingly and fixedly connected with a micro-interface generator The reactor comprises a plurality of micro-interface generator units (5) which are sequentially and uniformly distributed along an annular catalyst interlayer (16), the micro-interface generator units (5) are sequentially spliced to form an annular structure matched with the annular catalyst interlayer (16), each micro-interface generator unit (5) is respectively communicated with a propylene gas supply device through a propylene gas inlet branch pipe (6) penetrating through the side wall of the reactor (1), the top surface of each micro-interface generator unit (5), one side end surface facing the axis of the reactor (1) and the end surface between every two adjacent micro-interface generator units (5) are respectively and fixedly connected with a sealing plate B (18), the side wall of the reactor (1) and the end surface positioned in a mixing area B (3') are respectively communicated with a plurality of pure water liquid inlet branch pipes (7), and the pure water inlet branch pipes (7) are uniformly distributed by taking the axis of the reactor (1) as the center, the feed liquor direction that pure water feed liquor branch pipe (7) got into reactor (1) is the tangential direction of reactor (1) corresponding position department, and the angular velocity direction of intaking when getting into reactor (1) through pure water feed liquor branch pipe (7) is the same, pure water feed liquor branch pipe (7) communicate with pure water supply installation respectively.

3. The reactor for improving the hydration reaction of propylene according to claim 1 or 2, wherein: micron-sized bubbles generated by propylene gas of the propylene gas inlet branch pipe (6) through the micro-interface generator unit (5) are perpendicular to the direction of the annular catalyst interlayer (16), downwards penetrate through the annular catalyst interlayer (16), and then upwards penetrate through the central catalyst interlayer (17), the annular catalyst interlayer (16) and the central catalyst interlayer (17) both comprise multiple layers of wire meshes A, and a catalyst layer is supposed to be fixed between every two adjacent layers of wire meshes A.

4. The reactor for improving the hydration reaction of propylene according to claim 3, wherein: the annular catalyst barrier layer (16) is inclined upwards along the direction from outside to inside.

5. The reactor for improving the hydration reaction of propylene according to claim 2, wherein: the propylene gas inlet branch pipe (6) corresponding to the micro-interface generator unit (5) fixed on the catalyst interlayer A (2) and the propylene gas inlet branch pipe (6) corresponding to the micro-interface generator unit (5) fixed on the catalyst interlayer B (2') are respectively communicated with a propylene gas supply device through respective gas inlet circular pipes (10).

6. The reactor for improving the hydration reaction of propylene according to claim 5, wherein: the pure water inlet branch pipe (7) correspondingly positioned at the position of the mixing area A (3) and the pure water inlet branch pipe (7) correspondingly positioned at the position of the mixing area B (3') are respectively communicated with a pure water supply device through respective liquid inlet circular pipes (11).

7. The reactor for improving the hydration reaction of propylene according to claim 6, wherein: the utility model discloses a reactor, including reactor (1), the position department that is located and is connected with reactor (1) is fixed with axle center cladding respectively to the lateral wall of pure water feed liquor branch pipe (7), airtight pipe box (12) are respectively through breather pipe (13) and the adjacent air inlet ring pipe (10) intercommunication in mixing area top of this pure water feed liquor branch pipe (7) to the pipe wall of pure water feed liquor branch pipe (7), be equipped with inlet port (21) corresponding to airtight pipe box (12) position department, inlet port (21) still are equipped with can be the check valve that the propylene gas in pipe box (12) gets into in pure water feed liquor branch pipe (7).

8. The reactor for increasing the effect of hydration reaction of propylene according to claim 7, wherein: the air inlets (21) are provided with a plurality of groups along the length direction of the pure water liquid inlet branch pipes (7), each group of air inlets (21) is provided with a plurality of air inlets which are uniformly distributed by taking the axes of the pure water liquid inlet branch pipes (7) as the center, and two adjacent groups of air inlets (21) are arranged in a staggered manner.

9. The reactor for increasing the effect of hydration reaction of propylene according to claim 8, wherein: the inner wall of the pure water liquid inlet branch pipe (7) is uniformly provided with a plurality of rib plates (22) which are spirally arranged along the axial direction of the pure water liquid inlet branch pipe (7), two adjacent rib plates (22) form a spiral channel, and the air inlet holes (21) are respectively and correspondingly positioned in the spiral channel.

10. The reactor for improving the hydration reaction of propylene according to claim 6, wherein: the axle center of pure water feed liquor branch pipe (7) is along pure water inlet direction downward sloping, pure water feed liquor branch pipe (7) forms inlet (9) with the lateral wall junction of reactor (1), inlet (9) still respectively fixedly connected with silk screen B (14).

Technical Field

The invention relates to the technical field of preparation of isopropanol by propylene hydration reaction, in particular to a reactor for improving propylene hydration reaction effect.

Background

Isopropanol is an organic compound with the molecular formula C3H8O, an isomer of n-propanol, known as dimethyl methanol, 2-propanol, also known in the industry as IPA. Is a colorless transparent liquid, is flammable and has an odor similar to a mixture of ethanol and acetone. It is soluble in water, and also soluble in many organic solvents such as alcohol, ether, benzene, chloroform, etc. Isopropanol is an important chemical product and raw material.

There are generally three methods for producing isopropanol: indirect hydration, direct hydration and acetone hydrogenation. Of the three methods, the direct hydration method is the most environmentally friendly method and the process flow is the simplest method. The propanol is produced by direct hydration of propylene and water under certain pressure and temperature and under the action of catalyst. The direct hydration process suffers from the disadvantages of relatively low propylene conversion and large propylene recycle, which can now be improved by modifying some of the process conditions. However, no matter what process is adopted to produce the isopropanol by the direct hydration method of the propylene, the conversion rate of the propylene in the corresponding process needs to be ensured, the better the mixing effect of the propylene and the water is, the higher the conversion rate of the propylene is, and the higher the yield of the isopropanol is. The technical problem of the mixing effect of propylene and water is still greatly improved by those skilled in the art.

Disclosure of Invention

The invention aims to: the reactor overcomes the defects of the prior art, and provides a reactor for improving the propylene hydration reaction effect, and micron-sized propylene bubbles generated by a micro-interface generator are mixed with an annular catalyst interlayer and a central catalyst interlayer to form emulsion which is convenient to react to generate isopropanol when passing through the annular catalyst interlayer and then react to generate isopropanol when passing through the central catalyst interlayer, so that the propylene hydration reaction effect is improved, and the yield of the isopropanol is improved; the pure water liquid inlet branch pipe is connected with the reactor, so that a gas-liquid mixture in the reactor can automatically stir and mix under the liquid inlet effect of the liquid inlet branch pipe, and the mixing effect of the gas-liquid mixture is improved; through the structure of the pure water liquid inlet branch pipe, a gas-liquid mixture which is directly premixed enters the reactor, and the reaction efficiency of the hydration reaction of the propylene gas in the reactor is further improved; the reactor forms a multi-stage mixing area through a plurality of catalyst interlayers, so that propylene gas in the reactor has more chances to generate hydration reaction, the effect of propylene hydration reaction is further improved, and the yield of isopropanol is improved; the gas-liquid mixture that pure water feed liquor branch pipe was advanced can take away the micron order propylene bubble that remains in annular catalyst interlayer and its and water mixture formation emulsion that mixes and react with central catalyst interlayer after with the gas-liquid mixture in the mixed zone, still is convenient for make little interfacial generator continue to produce more micron order propylene bubbles and the emulsion that forms with water mixture simultaneously can react with annular catalyst interlayer.

The technical scheme adopted by the invention is as follows:

improve reactor of propylene hydration reaction effect, including the reactor, fixedly connected with catalyst interlayer A in the reactor, catalyst interlayer A separates the mixed zone A that is located catalyst interlayer A below and the escape area who is located catalyst interlayer A top in with the reactor in, catalyst interlayer A is including the annular catalyst interlayer that is fixed in the reactor inside wall and the central catalyst interlayer that is fixed in annular catalyst interlayer inboard through closing plate A, seal through closing plate A between annular catalyst interlayer and the central catalyst interlayer and cut off, the inside wall of reactor, the correspondence is located the corresponding fixedly connected with micro-interface generator of annular catalyst interlayer top surface, micro-interface generator includes a plurality of micro-interface generator units along annular catalyst interlayer evenly distributed in proper order, micro-interface generator unit splices in proper order, the, Forming an annular structure matched with the annular catalyst interlayer, wherein each micro-interface generator unit is respectively communicated with a propylene gas supply device through a propylene gas inlet branch pipe penetrating through the side wall of the reactor, the top surface of the micro-interface generator unit, the end surface of one side facing the axis of the reactor and the end surface between two adjacent micro-interface generator units are fixedly connected with a sealing plate B, the side wall of the reactor and the mixing area A are respectively communicated with a plurality of pure water liquid inlet branch pipes which are uniformly distributed by taking the axis of the reactor as the center, the liquid inlet direction of the pure water liquid inlet branch pipe entering the reactor is the tangential direction of the corresponding position of the reactor, the angular velocity direction of intaking when getting into the reactor through pure water feed liquor branch pipe is the same, pure water feed liquor branch pipe communicates with pure water supply installation respectively, the top of reactor still is equipped with the outlet duct.

The invention has the further improvement scheme that a catalyst interlayer B is fixedly connected in the reactor and positioned below the catalyst interlayer A, the catalyst interlayer B divides a mixing zone A in the reactor into a mixing zone B positioned between the catalyst interlayer A and the catalyst interlayer B, the catalyst interlayer B has the same structure as the catalyst interlayer A, and also comprises an annular catalyst interlayer fixed on the inner side wall of the reactor and a central catalyst interlayer fixed on the inner side of the annular catalyst interlayer through a sealing plate A, the annular catalyst interlayer and the central catalyst interlayer are sealed and separated through the sealing plate A, the inner side wall of the reactor and the top surface of the annular catalyst interlayer corresponding to the catalyst interlayer B are also correspondingly and fixedly connected with a micro-interface generator, and the micro-interface generator comprises a plurality of micro-interface generator units which are sequentially and uniformly distributed along the annular catalyst interlayer, the micro-interface generator units are sequentially spliced to form an annular structure matched with the annular catalyst interlayer, each micro-interface generator unit is respectively communicated with a propylene gas supply device through a propylene gas inlet branch pipe penetrating through the side wall of the reactor, the top surface of the micro-interface generator unit, the end surface of one side facing the axis of the reactor and the end surface between two adjacent micro-interface generator units are fixedly connected with a sealing plate B, the side wall of the reactor and the mixing area B are respectively communicated with a plurality of pure water liquid inlet branch pipes which are uniformly distributed by taking the axis of the reactor as the center, the liquid inlet direction of the pure water liquid inlet branch pipe entering the reactor is the tangential direction of the corresponding position of the reactor, the water inlet angular velocity direction when entering the reactor through the pure water liquid inlet branch pipe is the same, and the pure water liquid inlet branch pipe is respectively communicated with a pure water supply device.

According to a further improvement scheme of the invention, micron-sized bubbles generated by propylene gas of the propylene gas inlet branch pipe through the micro-interface generator unit are perpendicular to the direction of the annular catalyst interlayer, downwards penetrate through the annular catalyst interlayer, and then upwards penetrate through the central catalyst interlayer, the annular catalyst interlayer and the central catalyst interlayer both comprise a plurality of layers of wire nets A, and a catalyst layer is supposed to be fixed between two adjacent layers of wire nets A.

In a further development of the invention, the annular catalyst barrier is inclined upwards in the direction from the outside to the inside.

The invention has the further improvement scheme that the propylene gas inlet branch pipe corresponding to the micro-interface generator unit fixed on the catalyst interlayer A and the propylene gas inlet branch pipe corresponding to the micro-interface generator unit fixed on the catalyst interlayer B are respectively communicated with a propylene gas supply device through respective gas inlet circular pipes.

The invention has the further improvement scheme that the pure water liquid inlet branch pipe correspondingly positioned at the position of the mixing area A and the pure water liquid inlet branch pipe correspondingly positioned at the position of the mixing area B are respectively communicated with a pure water supply device through respective liquid inlet circular pipes.

According to a further improvement scheme of the invention, the outer side wall of the pure water liquid inlet branch pipe and the position connected with the reactor are respectively and coaxially coated and fixed with a closed pipe sleeve, the closed pipe sleeves are respectively communicated with an adjacent air inlet ring pipe above a mixing area where the pure water liquid inlet branch pipe is located through an air pipe, an air inlet hole is formed in the pipe wall of the pure water liquid inlet branch pipe and corresponds to the position of the closed pipe sleeve, and a check valve capable of enabling propylene gas in the pipe sleeve to enter the pure water liquid inlet branch pipe is further arranged on the air inlet hole.

According to a further improvement scheme of the invention, multiple groups of the air inlets are arranged along the length direction of the pure water inlet branch pipe, multiple air inlets are arranged in each group and are uniformly distributed by taking the axis of the pure water inlet branch pipe as the center, and two adjacent groups of the air inlets are arranged in a staggered manner.

According to a further improvement scheme of the invention, a plurality of rib plates spirally arranged along the axial direction of the pure water liquid inlet branch pipe are uniformly distributed on the inner wall of the pure water liquid inlet branch pipe, two adjacent rib plates form a spiral channel, and the air inlet holes are respectively and correspondingly positioned in the spiral channel.

According to a further improvement scheme of the invention, the axes of the pure water liquid inlet branch pipes are inclined downwards along the pure water liquid inlet direction, liquid inlets are formed at the joints of the pure water liquid inlet branch pipes and the side walls of the reactor, and the liquid inlets are respectively and fixedly connected with a wire mesh B.

The invention has the further improvement scheme that the water inlet direction of the pure water inlet branch pipe corresponding to the mixing area A is the same as or opposite to the water inlet direction of the pure water inlet branch pipe corresponding to the mixing area B.

According to a further improvement scheme of the invention, the gas inlet circular pipes are fixedly connected through connecting pipes A, the gas inlet circular pipes are coaxially arranged at the outer side of the reactor, and the connecting pipes A are arranged in plurality and uniformly distributed by taking the axis of the reactor as the center.

In a further improvement of the invention, the air inlet ring pipes are communicated through a connecting pipe A.

According to a further improvement scheme of the invention, the liquid inlet circular pipes are fixedly connected through connecting pipes B, the liquid inlet circular pipes are coaxially arranged on the outer side of the reactor, and the connecting pipes B are arranged in plurality and uniformly distributed by taking the axis of the reactor as the center.

In a further improvement of the invention, the liquid inlet ring pipes are communicated through a connecting pipe B.

The invention has the beneficial effects that:

first, the reactor for improving the propylene hydration reaction effect of the present invention is provided with the micro interface generator, the annular catalyst interlayer and the central catalyst interlayer, so that the micron-sized propylene bubbles generated by the micro interface generator and the pure water in the reactor are mixed to form an emulsion, which is reacted to generate isopropanol when passing through the annular catalyst interlayer and then is reacted to generate isopropanol when passing through the central catalyst interlayer, thereby improving the propylene hydration reaction effect and the isopropanol yield.

Secondly, the reactor for improving the propylene hydration reaction effect is connected with the reactor through the pure water liquid inlet branch pipe, so that the gas-liquid mixture in the reactor can automatically play a role in stirring and mixing under the liquid inlet effect of the liquid inlet branch pipe, and the mixing effect of the gas-liquid mixture is improved.

Thirdly, the reactor for improving the hydration reaction effect of the propylene further improves the reaction efficiency of the hydration reaction of the propylene gas in the reactor by the structure of the pure water liquid inlet branch pipe, so that a directly premixed gas-liquid mixture enters the reactor.

Fourthly, the reactor for improving the propylene hydration reaction effect of the invention forms a multi-stage mixing area through a plurality of catalyst separation layers, so that propylene gas in the reactor has more chances to generate hydration reaction, further improving the propylene hydration reaction effect and improving the yield of isopropanol.

Fifthly, according to the reactor for improving the propylene hydration reaction effect, the gas-liquid mixture fed by the pure water liquid inlet branch pipe can take away micron-sized propylene bubbles remaining in the annular catalyst interlayer and the micron-sized propylene bubbles mixed with water to form an emulsion, and the micron-sized propylene bubbles are mixed with the gas-liquid mixture in the mixing area and then react with the central catalyst interlayer, and meanwhile, the micro-interface generator can continuously generate more micron-sized propylene bubbles and the emulsion formed by mixing the micron-sized propylene bubbles with water can react with the annular catalyst interlayer.

Description of the drawings:

FIG. 1 is a schematic sectional front view of a reactor according to the present invention.

FIG. 2 is an enlarged sectional view of the joint between the pure water inlet pipe and the reactor according to the present invention.

The specific implementation mode is as follows:

as can be seen from fig. 1 and 2, the reactor for improving the propylene hydration reaction effect comprises a reactor 1, a catalyst barrier a2 is fixedly connected in the reactor 1, the catalyst barrier a2 divides the interior of the reactor 1 into a mixing zone A3 located below a catalyst barrier a2 and an escape zone 4 located above the catalyst barrier a2, the catalyst barrier a2 comprises an annular catalyst barrier 16 fixed on the inner side wall of the reactor 1 and a central catalyst barrier 17 fixed on the inner side of the annular catalyst barrier 16 through a sealing plate a15, the annular catalyst barrier 16 and the central catalyst barrier 17 are sealed and separated through the sealing plate a15, a micro-interface generator is correspondingly and fixedly connected to the inner side wall of the reactor 1 and the top surface of the annular catalyst barrier 16, the micro-interface generator comprises a plurality of micro-interface generator units 5 which are sequentially and uniformly distributed along the annular catalyst barrier 16, the micro-interface generator units 5 are sequentially spliced and form an annular structure matched with the annular catalyst interlayer 16, each micro-interface generator unit 5 is respectively communicated with a propylene gas supply device through a propylene gas inlet branch pipe 6 penetrating through the side wall of the reactor 1, the top surface of each micro-interface generator unit 5, one side end surface facing the axis of the reactor 1 and the end surface between two adjacent micro-interface generator units 5 are respectively and fixedly connected with a sealing plate B18, the side wall of the reactor 1 is also respectively communicated with a plurality of pure water liquid inlet branch pipes 7 in a mixing area A3, the pure water liquid inlet branch pipes 7 are uniformly distributed by taking the axis of the reactor 1 as the center, the liquid inlet direction of each pure water liquid inlet branch pipe 7 entering the reactor 1 is the tangential direction of the corresponding position of the reactor 1, and the water inlet angular speed direction when entering the reactor 1 through the pure water inlet branch pipes 7 is the same, the pure water inlet branch pipes 7 are respectively communicated with a pure water supply device, and the top of the reactor 1 is also provided with an air outlet pipe 8.

A catalyst partition layer B2 'is fixedly connected in the reactor 1 below the catalyst partition layer A2, the catalyst partition layer B2' divides the mixing zone A3 in the reactor 1 into a mixing zone B3 'between the catalyst partition layer A2 and the catalyst partition layer B2', the catalyst partition layer B2 'has the same structure as the catalyst partition layer A2, the reactor also comprises an annular catalyst partition layer 16 fixed on the inner side wall of the reactor 1 and a central catalyst partition layer 17 fixed on the inner side of the annular catalyst partition layer 16 through a sealing plate A15, the annular catalyst partition layer 16 and the central catalyst partition layer 17 are sealed and separated through the sealing plate A15, a micro-interface generator is correspondingly and fixedly connected to the inner side wall of the reactor 1 and the top surface of the annular catalyst partition layer 16 corresponding to the catalyst partition layer B2', the micro-interface generator comprises a plurality of micro-interface generator units 5 which are sequentially and uniformly distributed along the annular catalyst partition layer 16, the micro-interface generator units 5 are sequentially spliced and form an annular structure matched with the annular catalyst interlayer 16, each micro-interface generator unit 5 is respectively communicated with a propylene gas supply device through a propylene gas inlet branch pipe 6 passing through the side wall of the reactor 1, the top surface of each micro-interface generator unit 5, one side end surface facing the axis of the reactor 1 and the end surface between two adjacent micro-interface generator units 5 are respectively and fixedly connected with a sealing plate B18, the side wall of the reactor 1 is also respectively communicated with a plurality of pure water liquid inlet branch pipes 7 in a mixing area B3', the pure water liquid inlet branch pipes 7 are uniformly distributed by taking the axis of the reactor 1 as the center, the liquid inlet direction of each pure water liquid inlet branch pipe 7 entering the reactor 1 is the tangential direction of the corresponding position of the reactor 1, and the water inlet angular velocity direction when the pure water inlet branch pipes 7 enter the reactor 1 is the same, and the pure water inlet branch pipes 7 are respectively communicated with a pure water supply device.

Micron-sized bubbles generated by the propylene gas of the propylene gas inlet branch pipe 6 through the micro-interface generator unit 5 are perpendicular to the direction of the annular catalyst interlayer 16, downwards pass through the annular catalyst interlayer 16, and then upwards pass through the central catalyst interlayer 17, the annular catalyst interlayer 16 and the central catalyst interlayer 17 both comprise a plurality of layers of wire meshes A, and a catalyst layer is supposed to be fixed between two adjacent layers of wire meshes A.

The annular catalyst barrier 16 slopes upward in the outside-in direction.

The propylene gas inlet branch pipe 6 corresponding to the micro-interface generator unit 5 fixed on the catalyst isolation layer A2 and the propylene gas inlet branch pipe 6 corresponding to the micro-interface generator unit 5 fixed on the catalyst isolation layer B2' are respectively communicated with a propylene gas supply device through respective gas inlet circular pipes 10.

The pure water inlet branch pipe 7 correspondingly positioned at the position of the mixing area A3 and the pure water inlet branch pipe 7 correspondingly positioned at the position of the mixing area B3' are respectively communicated with a pure water supply device through respective liquid inlet loop pipes 11.

The outer side wall of the pure water liquid inlet branch pipe 7 and the positions connected with the reactor 1 are respectively fixed with a sealed pipe sleeve 12 in a coaxial coating mode, the sealed pipe sleeves 12 are respectively communicated with an air inlet ring pipe 10 adjacent to the upper portion of a mixing area where the pure water liquid inlet branch pipe 7 is located through an air vent pipe 13, an air inlet hole 21 is formed in the position, corresponding to the sealed pipe sleeve 12, of the pipe wall of the pure water liquid inlet branch pipe 7, and the air inlet hole 21 is further provided with a one-way valve capable of enabling propylene gas in the pipe sleeve 12 to enter the pure water liquid inlet branch pipe 7.

The air inlet holes 21 are provided with a plurality of groups along the length direction of the pure water inlet branch pipe 7, each group of air inlet holes 21 is provided with a plurality of air inlet holes and is uniformly distributed by taking the axis of the pure water inlet branch pipe 7 as the center, and two adjacent groups of air inlet holes 21 are arranged in a staggered manner.

The inner wall of the pure water liquid inlet branch pipe 7 is uniformly distributed with a plurality of rib plates 22 which are spirally arranged along the axial direction of the pure water liquid inlet branch pipe 7, two adjacent rib plates 22 form a spiral channel, and the air inlet holes 21 are respectively and correspondingly positioned in the spiral channel.

The axle center of pure water inlet branch pipe 7 is along pure water inlet direction downward sloping, pure water inlet branch pipe 7 forms inlet 9 with the lateral wall junction of reactor 1, inlet 9 still respectively fixedly connected with silk screen B14.

The water inlet direction of the pure water inlet branch pipe 7 correspondingly positioned in the mixing area A3 is the same as or opposite to the water inlet direction of the pure water inlet branch pipe 7 correspondingly positioned in the mixing area B3'. If the water inlet directions are the same, the pure water inlet branch pipe 7 of the mixing area A3 and the pure water inlet branch pipe 7 of the mixing area B3' are conveniently connected and fixed; the opposite direction of the water feeding facilitates further improvement of the mixing effect of propylene and pure water in the mixing zone B3'.

The gas inlet circular pipes 10 are fixedly connected through a connecting pipe A19, the gas inlet circular pipes 10 are coaxially arranged at the outer side of the reactor 1, and a plurality of connecting pipes A19 are uniformly distributed by taking the axis of the reactor 1 as the center.

The inlet ring pipes 10 are communicated with each other through a connecting pipe A19.

The liquid inlet loop 11 is fixedly connected with the liquid inlet loop 11 through a connecting pipe B20, the liquid inlet loop 11 is coaxially arranged at the outer side of the reactor 1, and a plurality of connecting pipes B20 are arranged and uniformly distributed by taking the axis of the reactor 1 as the center.

The liquid inlet loop pipe 11 is communicated with the connecting pipe B20.

When the device is used, pure water supplied by the pure water supply device is heated to the reaction temperature by controlling the pure water pipeline valve, and then only supplies water to the liquid inlet loop pipe 11 corresponding to the mixing area A3, and the liquid inlet loop pipe 11 supplies water through the corresponding liquid inlet branch pipe 7; meanwhile, the propylene gas supplied by the propylene gas supply device is heated to the reaction temperature through the control of a propylene pipeline valve, and then the propylene gas is supplied only through the gas inlet loop 10 corresponding to the mixing area A3, and the propylene gas is supplied into the closed sleeve 12 arranged on the outer side wall of the corresponding liquid inlet branch pipe 7 through the gas inlet loop 10 through the vent pipe 13; propylene gas enters the liquid inlet branch pipe 7 through the air inlet 21 under the action of air pressure, is rapidly mixed with pure water in the liquid inlet branch pipe 7, and enables the propylene gas and the pure water to have more relative movement opportunities in the radial direction and the circumferential direction of the liquid inlet branch pipe 7 under the action of power of spraying the propylene gas into the liquid inlet branch pipe 7 and the action of the spiral channel, so that the propylene gas and the pure water are more effectively mixed, and meanwhile, the propylene gas and the pure water can jointly move forwards along the spiral channel and enable a gas-liquid mixture of the propylene gas and the pure water to move in the reactor 1 in an accelerated manner along the axial direction of the liquid inlet branch pipe 7; when the gas-liquid mixture of the propylene gas and the pure water in the liquid inlet branch pipe 7 passes through the liquid inlet 9 formed at the joint of the liquid inlet branch pipe 7 and the reactor 1, the gas-liquid mixture of the propylene gas and the pure water moving at a high speed collides with the wire mesh B14 at the liquid inlet 9, so that the mixture of the pure water and the propylene gas is crushed into liquid drops and bubbles with smaller particles, and the propylene gas and the pure water are further mixed; the gas-liquid mixture entering the reactor 1 through the liquid inlet 9 rotates along the liquid inlet direction to form a vortex due to the liquid inlet direction of the liquid inlet 9, so that the mixing effect of the propylene gas and the pure water is further improved; the liquid inlet branch pipe 7 continuously inputs a gas-liquid mixture of propylene gas and pure water into the reactor 1, the liquid level of the gas-liquid mixture in the reactor 1 gradually rises, when the liquid level of the gas-liquid mixture rises to be contacted with the catalyst interlayer B2 'in the reactor 1, the gas-liquid mixture can start to react to generate isopropanol, the propylene gas escaping from the isopropanol and the gas-liquid mixture continuously and sequentially passes through the central catalyst interlayers 17 of the catalyst interlayer B2' and the catalyst interlayer A2, and then leaves the reactor 1 from the gas outlet pipe 8 at the top of the reactor 1 to carry out the subsequent process of separating the propylene gas and the isopropanol.

On the basis of the above process, when the liquid level of the gas-liquid mixture of propylene gas and pure water in the reactor 1 continues to flow upward over the catalyst partition layer B2'; then, the propylene gas heated to the reaction temperature is supplied to the micro-interface generator unit 5 corresponding to the catalyst barrier layer B2' through the propylene inlet branch pipe 6 corresponding to the mixing zone A3 by controlling a propylene pipeline valve; then, under the action of the micro-interface generator unit 5, the propylene gas generates a large amount of micron-sized bubbles in the gas-liquid mixture of the propylene gas and the pure water in the reactor 1, and forms an emulsion with the pure water in the gas-liquid mixture of the propylene gas and the pure water, the gas-liquid mixture of the propylene containing the emulsion and the micron-sized propylene bubbles and the pure water downwards passes through the annular catalyst interlayer 16 to react to generate isopropanol, and then the emulsion and the micron-sized bubbles remaining in the annular catalyst interlayer 16 leave the annular catalyst interlayer 16 under the vortex action of the gas-liquid mixture rotating in the mixing area a3, so that the micro-interface generator unit 5 further generates the micron-sized bubbles and forms an emulsion with the gas-liquid mixture of the propylene and the pure water; since the generated isopropyl alcohol is in a gaseous state, the gas content in the emulsion and the micron-sized bubbles is higher than that in most of the gas-liquid mixture in the mixing zone A3, the density of the isopropyl alcohol, the emulsion and the micron-sized bubbles is lower than that of the gas-liquid mixture, the inertia is lower, the isopropyl alcohol, the emulsion and the micron-sized bubbles are located at the upper layer of the gas-liquid mixture in the mixing zone A3, the annular catalyst barrier 16 of the catalyst barrier B2 ' is inclined upwards from outside to inside, the emulsion and the micron-sized bubbles which are vertical to the annular catalyst barrier 16 move towards the center of the reactor 1 while moving downwards, and since the top surface of the mixing zone A3 is the catalyst barrier B2 ', the isopropyl alcohol, the emulsion and the micron-sized bubbles in the mixing zone A3 are concentrated at the middle position of the upper layer of the gas-liquid mixture, namely, the central catalyst barrier 17 which exactly corresponds to the catalyst barrier B2 ', the emulsion and the micron-sized bubbles are blocked by the central catalyst interlayer 17 and are gathered in the central catalyst interlayer 17, so that the mixture of the emulsion, the micron-sized bubbles and pure water, which is formed by fully mixing propylene gas and pure water, is further conveniently contacted with the central catalyst interlayer 17 effectively, the reaction efficiency is improved, and the generated isopropanol can conveniently escape upwards through the central catalyst interlayer 17; propylene gas escaping from the mixture of isopropanol and gas-liquid which passes upwards through the catalyst barrier layer B2' continues to pass upwards through the central catalyst barrier layer 17 of each catalyst barrier layer A2 and then leaves the reactor 1 from the gas outlet pipe 8 at the top of the reactor 1 and is subjected to a subsequent process for separating propylene gas and isopropanol.

On the basis of the above process, when the yield of the isopropanol needs to be improved, pure water supplied by a pure water supply device is heated to the reaction temperature through the control of a pure water pipeline valve and the control of a propylene pipeline valve, and then the pure water is supplied to the liquid inlet loop pipe 11 corresponding to the mixing area B3', and the liquid inlet loop pipe 11 is supplied with water through the corresponding liquid inlet branch pipe 7; meanwhile, the propylene gas supplied by the propylene gas supply device is heated to the reaction temperature through the control of a propylene pipeline valve, and then is supplied through the gas inlet ring pipe 10 corresponding to the mixing area B3', and the gas inlet ring pipe 10 supplies the propylene gas into the closed sleeve 12 arranged on the outer side wall of the corresponding liquid inlet branch pipe 7 through the vent pipe 13; propylene gas enters the liquid inlet branch pipe 7 through the air inlet 21 under the action of air pressure, is rapidly mixed with pure water in the liquid inlet branch pipe 7, and enables the propylene gas and the pure water to have more relative movement opportunities in the radial direction and the circumferential direction of the liquid inlet branch pipe 7 under the action of power of spraying the propylene gas into the liquid inlet branch pipe 7 and the action of the spiral channel, so that the propylene gas and the pure water are more effectively mixed, and meanwhile, the propylene gas and the pure water can jointly move forwards along the spiral channel and enable a gas-liquid mixture of the propylene gas and the pure water to move in the reactor 1 in an accelerated manner along the axial direction of the liquid inlet branch pipe 7; when the gas-liquid mixture of the propylene gas and the pure water in the liquid inlet branch pipe 7 passes through the liquid inlet 9 formed at the joint of the liquid inlet branch pipe 7 and the reactor 1, the gas-liquid mixture of the propylene gas and the pure water moving at a high speed collides with the wire mesh B14 at the liquid inlet 9, so that the mixture of the pure water and the propylene gas is crushed into liquid drops and bubbles with smaller particles, and the propylene gas and the pure water are further mixed; the gas-liquid mixture entering the reactor 1 through the liquid inlet 9 rotates along the liquid inlet direction to form a vortex due to the liquid inlet direction of the liquid inlet 9, so that the mixing effect of the propylene gas and the pure water is further improved; the liquid inlet branch pipe 7 continuously inputs the gas-liquid mixture of the propylene gas and the pure water into the mixing zone B3 'of the reactor 1, and continuously feeds liquid and gas into the mixing zone A3, so that the liquid level of the gas-liquid mixture in the mixing zone B3' is rapidly raised, when the liquid level of the gas-liquid mixture rises to be in contact with the catalyst barrier a2 in the reactor 1, the gas-liquid mixture in the mixing zone A3 can react again to generate isopropanol, and the propylene gas escaping from the isopropanol and gas-liquid mixture continuously passes through the central catalyst barrier 17 of the catalyst barrier a2 upwards and then leaves the reactor 1 from the gas outlet pipe 8 at the top of the reactor 1, and then the subsequent process of separating the propylene gas and the isopropanol is carried out.

On the basis of the above process, when the liquid level of the gas-liquid mixture of propylene gas and pure water in the reactor 1 continues to flow upward over the catalyst separation layer a 2; then, the propylene gas heated to the reaction temperature is supplied to the micro-interface generator unit 5 corresponding to the catalyst barrier A2 through the propylene inlet branch pipe 6 corresponding to the mixing zone B3' under the control of a propylene pipeline valve; then, under the action of the micro-interface generator unit 5, the propylene gas generates a large amount of micron-sized bubbles in the gas-liquid mixture of the propylene gas and the pure water in the reactor 1, and forms an emulsion with the pure water in the gas-liquid mixture of the propylene gas and the pure water, the gas-liquid mixture of the propylene containing the emulsion and the micron-sized propylene bubbles and the pure water downwards passes through the annular catalyst interlayer 16 to react to generate isopropanol, and then the emulsion and the micron-sized bubbles remaining in the annular catalyst interlayer 16 leave the annular catalyst interlayer 16 under the vortex action of the gas-liquid mixture rotating in the mixing area a3, so that the micro-interface generator unit 5 further generates the micron-sized bubbles and forms an emulsion with the gas-liquid mixture of the propylene and the pure water; since the generated isopropyl alcohol is in a gaseous state, the gas content in the emulsion and the micron-sized bubbles is higher than that in most of the gas-liquid mixture in the mixing zone B3 ', the density of the isopropyl alcohol, the emulsion and the micron-sized bubbles is lower than that of the gas-liquid mixture, the inertia is lower, the isopropyl alcohol, the emulsion and the micron-sized bubbles are located at the upper layer of the gas-liquid mixture in the mixing zone B3', the annular catalyst barrier 16 of the catalyst barrier a2 is inclined upward from the outside to the inside, the emulsion and the micron-sized bubbles which are vertical to the annular catalyst barrier 16 also move toward the center of the reactor 1 while moving downward, and since the top surface of the mixing zone B3 'is the catalyst barrier a2, the isopropyl alcohol, the emulsion and the micron-sized bubbles in the mixing zone B3' are concentrated at the middle position of the upper layer of the gas-liquid mixture, namely, the central catalyst barrier 17 which is exactly corresponding to the catalyst barrier 2, the emulsion and the micron-sized bubbles are blocked by the central catalyst interlayer 17 and are gathered in the central catalyst interlayer 17, so that the mixture of the emulsion, the micron-sized bubbles and pure water, which is formed by fully mixing propylene gas and pure water, is further conveniently contacted with the central catalyst interlayer 17 effectively, the reaction efficiency is improved, and the generated isopropanol can conveniently escape upwards through the central catalyst interlayer 17; the propylene gas escaping from the mixture of isopropanol and gas-liquid which passes upwards through the catalyst barrier layer A2 continues to leave the reactor 1 upwards from the outlet pipe 8 at the top of the reactor 1 and is subjected to a subsequent process for separating propylene gas and isopropanol.