WO2021189638A1 - 一种浸没式丙烯水合微界面强化反应系统及工艺 - Google Patents

一种浸没式丙烯水合微界面强化反应系统及工艺 Download PDF

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WO2021189638A1
WO2021189638A1 PCT/CN2020/092755 CN2020092755W WO2021189638A1 WO 2021189638 A1 WO2021189638 A1 WO 2021189638A1 CN 2020092755 W CN2020092755 W CN 2020092755W WO 2021189638 A1 WO2021189638 A1 WO 2021189638A1
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micro
propylene
reactor
interface generator
catalyst
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PCT/CN2020/092755
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English (en)
French (fr)
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张志炳
周政
张锋
李磊
孟为民
王宝荣
杨高东
罗华勋
杨国强
田洪舟
曹宇
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南京延长反应技术研究院有限公司
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Priority to EP20927210.3A priority Critical patent/EP4129460A4/en
Priority to US17/617,949 priority patent/US11517868B2/en
Priority to JP2022555086A priority patent/JP7430304B2/ja
Publication of WO2021189638A1 publication Critical patent/WO2021189638A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B01J8/0257—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical annular shaped bed
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/03—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2
    • C07C29/04—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2 by hydration of carbon-to-carbon double bonds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2455—Stationary reactors without moving elements inside provoking a loop type movement of the reactants
    • B01J19/2465—Stationary reactors without moving elements inside provoking a loop type movement of the reactants externally, i.e. the mixture leaving the vessel and subsequently re-entering it
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0207—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0285—Heating or cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/48—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
    • B01J2204/002—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices the feeding side being of particular interest
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00176—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles outside the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00823—Mixing elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00823—Mixing elements
    • B01J2208/00831—Stationary elements
    • B01J2208/0084—Stationary elements inside the bed, e.g. baffles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00823—Mixing elements
    • B01J2208/00831—Stationary elements
    • B01J2208/00849—Stationary elements outside the bed, e.g. baffles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00893—Feeding means for the reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00938—Flow distribution elements
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the invention relates to the technical field of isopropanol preparation, in particular to a submerged propylene hydration micro-interface strengthening reaction system and process.
  • Alkenes can be converted into corresponding alcohols through hydration.
  • the commonly used methods are mainly indirect hydration and direct hydration.
  • the indirect hydration requires esterification and hydrolysis of olefins.
  • This reaction uses concentrated sulfuric acid as a medium, and the consumption of concentrated sulfuric acid is huge.
  • the waste liquid has a large amount of treatment and severely corrodes the equipment, so this method is basically no longer used in new industrial production equipment.
  • Isopropanol is a colorless, transparent and volatile liquid, miscible with water, but also soluble in alcohol, ether, benzene, chloroform, etc. It is soluble in organic and inorganic substances such as resin and rubber, and is similar to organic substances such as ethanol and acetone. Smell. Isopropanol has a wide range of industrial uses. It can be used as a chemical raw material to produce isopropyl ether, acetone, hydrogen peroxide, etc., and it can also be used as an efficient solvent to extract effective ingredients from natural substances. It is widely used in pharmaceutical production and other industries. It can be used as an additive for blending gasoline, detergent, dehydrating agent, antifreeze, etc. It can also be used as a skin care product and used in the cosmetics industry.
  • the gas-phase direct hydration method was first developed by the German Viba Company.
  • the existing gas-phase direct hydration method to produce isopropanol involves passing liquid propylene, deionized water and circulating propylene gas into the reactor together.
  • the reaction temperature is 180-260°C.
  • propylene gas reacts with deionized water to generate isopropanol under the action of a catalyst, and then the reaction product can be refined by processes such as water washing and rectification.
  • the present invention provides a submerged propylene hydration micro-interface strengthening reaction system and process to improve the efficiency of preparing isopropanol in the prior art.
  • the present invention provides a submerged propylene hydration micro-interface strengthening reaction system, which includes:
  • the reactor is used to provide a reaction place for deionized water and propylene to prepare isopropanol.
  • a catalyst placer is arranged in the reactor, and the catalyst placer is cylindrical and coaxial with the reactor. Small holes are evenly arranged on the inner and outer side walls of the placer, the upper and lower end faces of the catalyst placer are closed by annular blind plates, the cavity of the catalyst placer is loaded with catalyst, and the catalyst placer is immersed in the reaction Among them, the reactor is composed of a fully mixed flow reaction zone and a reflux reaction zone; the fully mixed flow reaction zone is arranged below the reactor for loading deionized water, propylene and catalyst and is used for propylene hydration reaction Provide a reaction space; the reflux reaction zone, which is arranged above the reactor, is used to reflux unreacted propylene and make the unreacted propylene react with deionized water again;
  • the micro-interface generator converts the pressure energy of the gas and/or the kinetic energy of the liquid into the surface energy of the bubble and transmits it to the gas reactant, and breaks the gas reactant propylene to form micron-sized bubbles with a diameter of ⁇ 1 ⁇ m and ⁇ 1mm to improve The mass transfer area between the gas reactant and the liquid reactant, reduces the thickness of the liquid film, and reduces the mass transfer resistance;
  • a circulation unit which is connected to the reactor and the micro-interface generator, is used to adjust the temperature of the reactants in the reactor, provide entrainment power for the micro-interface generator, and provide The reaction material is circulated from the inside of the catalyst holder to outside the catalyst holder to provide circulation power, so that the reactants and the catalyst are fully contacted.
  • micro-interface generator includes:
  • the first micro-interface generator is a pneumatic micro-interface generator, the first micro-interface generator is located in the fully mixed flow reaction zone in the reactor, and the first micro-interface generator is used to break propylene into micron scale After the crushing is completed, the micron-level bubbles are output to the fully mixed flow reaction zone in the reactor and the deionized water in the fully mixed flow reaction zone in the reactor is mixed to form a gas-liquid emulsion;
  • the second micro-interface generator is a hydraulic micro-interface generator, the second micro-interface generator is located in the reflux reaction zone in the reactor, and the second micro-interface generator is used for crushing and entraining the reaction
  • the unreacted propylene in the upper part of the reflux reaction zone in the vessel forms micron-scale micron-scale bubbles, which are mixed with deionized water to form a gas-liquid emulsion, and the gas-liquid emulsion is output to the fully mixed flow reaction zone to interact with the
  • the gas-liquid emulsion output by the first micro-interface generator is offset, so that unreacted propylene participates in the reaction again.
  • the inner and outer side walls of the catalyst placer are made of stainless steel wire mesh.
  • the second micro-interface generator is located inside the catalyst placer.
  • a first propylene transmission pipe, a propylene transmission main pipe, and a deionized water transmission pipe are arranged in the fully mixed flow reaction zone, and a first pump body is installed on the propylene transmission main pipe.
  • the ends are respectively connected with the first micro-interface generator and the propylene transmission manifold, and the first pump body is used to transport propylene along the propylene transmission manifold and the first propylene transmission pipe to the first micro-interface Generator;
  • the deionized water transmission pipe is installed with a third pump body, the third pump body will be deionized water along the deionized water transmission pipe into the reactor.
  • a second propylene transmission pipe, a return pipe, and a tail gas discharge pipe are arranged in the reflux reaction zone; two ends of the second propylene transmission pipe are connected to the propylene transmission main pipe and the second micro-interface generator respectively.
  • One end of the reflux pipe is connected to the third micro-interface generator, the other end of the reflux pipe is located in the upper part of the reflux reaction zone, and the reflux pipe is used to transfer unreacted propylene to the first Two micro-interface generators; the tail gas discharge pipe is used to discharge the tail gas in the reactor.
  • the circulation unit includes a heat exchanger and a second pump body, and the second pump body is used to extract the product in the reactor into the heat exchanger for heat exchange, and then discharge the product.
  • the second micro-interface generator provides entrainment power and circulating power for the reaction materials in the reactor to circulate from the inside of the catalyst holder to the outside of the catalyst holder, so that the reactants and the catalyst are fully contacted.
  • the present invention provides a submerged propylene hydration micro-interface strengthening reaction process, which includes:
  • Step 1 Working by the third pump body, transfer deionized water to the reactor along the deionized water transfer pipe;
  • Step 2 Through the work of the first pump body, propylene is transferred to the first micro-interface generator along the propylene transfer manifold and the first propylene transfer pipe, and at the same time along the propylene transfer manifold and the first micro-interface generator.
  • the two propylene transmission pipe is transmitted to the second micro-interface generator;
  • Step 3 The first micro-interface generator works to break propylene into micron-sized micro-sized bubbles, and after the crushing is completed, the micro-sized bubbles are output to the fully mixed flow reaction zone in the reactor and the reactor.
  • the deionized water in the fully mixed flow reaction zone is mixed to form a gas-liquid emulsion;
  • the second micro-interface generator works to break and entrain the unreacted propylene in the upper part of the reflux reaction zone in the reactor to form micron-scale micron-scale bubbles, Mix the micron-sized bubbles with deionized water to form a gas-liquid emulsion and output the gas-liquid emulsion to the fully mixed flow reaction zone to counteract the gas-liquid emulsion output from the first micro-interface generator to make unreacted
  • the propylene in the reactor again participates in the reaction;
  • the gas-liquid emulsion of propylene and deionized water in the reactor is in contact with the catalyst holder and reacts to produce isoprop
  • Step 4 In step 3, the remaining tail gas in the reactor is discharged along the tail gas exhaust pipe for subsequent tail gas treatment;
  • Step 5 In step 3, with the production of isopropanol, the circulation unit operates to exchange heat treatment for the product, adjust the temperature of the reactants in the reactor, provide entrainment power for the micro-interface generator, and The reaction materials in the reactor are circulated from the inside of the catalyst holder to outside the catalyst holder to provide circulating power.
  • the temperature in the reactor is 170-180°C, and the pressure is 1.7-2.0Mpa.
  • the beneficial effect of the present invention is that the present invention breaks the propylene gas to form micro-scale micro-sized bubbles, which have physical and chemical properties that conventional bubbles do not have.
  • the volume and surface area of the sphere are calculated The formula shows that when the total volume is constant, the total surface area of the bubbles is inversely proportional to the diameter of a single bubble. It can be seen that the total surface area of the micron-sized bubbles is huge, and the micron-sized bubbles are mixed with deionized water to form a gas-liquid emulsion. Increase the contact area of the gas-liquid two-phase, and achieve the effect of enhancing mass transfer within the lower preset operating conditions, effectively improving the conversion rate and efficiency of preparing isopropanol;
  • a reactor is used to provide a reaction place for deionized water and propylene to prepare isopropanol
  • a catalyst placer is arranged in the reactor, and the catalyst placer is cylindrical and coaxial with the reactor,
  • the inner and outer side walls of the catalyst placer are respectively uniformly provided with small holes, the upper and lower end faces of the catalyst placer are closed by annular blind plates, the cavity of the catalyst placer is loaded with catalyst, and the catalyst placer Submerged in the reactants, the reactor is composed of a fully mixed flow reaction zone and a reflux reaction zone; the fully mixed flow reaction zone is set below the reactor for loading deionized water, propylene and catalyst and is The propylene hydration reaction provides a reaction space; the reflux reaction zone, which is arranged above the reactor, is used to reflux unreacted propylene and make the unreacted propylene react with deionized water again;
  • the micro-interface generator converts the pressure energy of the gas and/or the kinetic energy of the liquid into the surface energy of the bubble and transmits it to the gas reactant, and breaks the gas reactant propylene to form micron-sized bubbles with a diameter of ⁇ 1 ⁇ m and ⁇ 1mm to improve The mass transfer area between the gas reactant and the liquid reactant, reduces the thickness of the liquid film, and reduces the mass transfer resistance;
  • a circulation unit which is connected to the reactor and the micro-interface generator, is used to adjust the temperature of the reactants in the reactor, provide entrainment power for the micro-interface generator, and provide The reaction material is circulated from the inside of the catalyst holder to outside the catalyst holder to provide circulation power, so that the reactants and the catalyst are fully contacted.
  • micro-interface generator includes:
  • the first micro-interface generator is a pneumatic micro-interface generator, the first micro-interface generator is located in the fully mixed flow reaction zone in the reactor, and the first micro-interface generator is used to break propylene into micron scale After the crushing is completed, the micron-level bubbles are output to the fully mixed flow reaction zone in the reactor and the deionized water in the fully mixed flow reaction zone in the reactor is mixed to form a gas-liquid emulsion;
  • the second micro-interface generator is a hydraulic micro-interface generator, the second micro-interface generator is located in the reflux reaction zone in the reactor, and the second micro-interface generator is used for crushing and entraining the reaction
  • the unreacted propylene in the upper part of the reflux reaction zone in the vessel forms micron-scale micron-scale bubbles, which are mixed with deionized water to form a gas-liquid emulsion, and the gas-liquid emulsion is output to the fully mixed flow reaction zone to interact with the
  • the gas-liquid emulsion output by the first micro-interface generator is offset, so that unreacted propylene participates in the reaction again.
  • the gas-liquid emulsions of propylene and deionized water in the reactor are in full contact with the catalyst holder, which further improves the single-pass conversion rate of propylene.
  • the inner and outer side walls of the catalyst placer are made of stainless steel wire mesh. Both the inner and outer sides of the cylindrical catalyst holder can expose the catalyst, so that the gas-liquid emulsion of propylene and deionized water in the reactor is in full contact with the catalyst holder, and the single-pass conversion rate of propylene is further improved.
  • the second micro-interface generator is located inside the catalyst placer.
  • a first propylene transmission pipe, a propylene transmission main pipe, and a deionized water transmission pipe are arranged in the fully mixed flow reaction zone, and a first pump body is installed on the propylene transmission main pipe.
  • the ends are respectively connected with the first micro-interface generator and the propylene transmission manifold, and the first pump body is used to transport propylene along the propylene transmission manifold and the first propylene transmission pipe to the first micro-interface Generator;
  • the deionized water transmission pipe is installed with a third pump body, the third pump body will be deionized water along the deionized water transmission pipe into the reactor.
  • a second propylene transmission pipe, a return pipe, and a tail gas discharge pipe are arranged in the reflux reaction zone; two ends of the second propylene transmission pipe are connected to the propylene transmission main pipe and the second micro-interface generator respectively.
  • One end of the reflux pipe is connected to the third micro-interface generator, the other end of the reflux pipe is located in the upper part of the reflux reaction zone, and the reflux pipe is used to transfer unreacted propylene to the first Two micro-interface generators; the tail gas discharge pipe is used to discharge the tail gas in the reactor.
  • the circulation unit includes a heat exchanger and a second pump body, and the second pump body is used to extract the product in the reactor into the heat exchanger for heat exchange, and then discharge the product.
  • the second micro-interface generator provides entrainment power and circulating power for the reaction materials in the reactor to circulate from the inside of the catalyst holder to the outside of the catalyst holder, so that the reactants and the catalyst are fully contacted.
  • Fig. 1 is a schematic structural diagram of an immersed propylene hydration micro-interface strengthening reaction system according to the present invention.
  • the terms “installed”, “connected”, and “connected” should be understood in a broad sense. For example, they can be fixed or fixed. It is a detachable connection or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the internal communication between two components.
  • installed e.g., they can be fixed or fixed. It is a detachable connection or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the internal communication between two components.
  • the specific meaning of the above-mentioned terms in the present invention can be understood according to specific circumstances.
  • FIG. 1 provides a submerged propylene hydration micro-interface strengthening reaction system of the present invention, including:
  • the reactor 1 is used to provide a reaction place for deionized water and propylene to prepare isopropanol.
  • a catalyst placer 2 is provided in the reactor, and the catalyst placer is cylindrical and coaxial with the reactor.
  • the inner and outer side walls of the catalyst placer are respectively uniformly provided with small holes, the upper and lower end faces of the catalyst placer are closed by annular blind plates, the cavity of the catalyst placer is loaded with catalyst, and the catalyst placer is immersed Among the reactants, the reactor is composed of a fully mixed flow reaction zone 3 and a reflux reaction zone 4; the fully mixed flow reaction zone is arranged below the reactor for loading deionized water, propylene, and catalyst.
  • the micro-interface generator converts the pressure energy of the gas and/or the kinetic energy of the liquid into the surface energy of the bubble and transmits it to the gas reactant, and breaks the gas reactant propylene to form micron-sized bubbles with a diameter of ⁇ 1 ⁇ m and ⁇ 1mm to improve The mass transfer area between the gas reactant and the liquid reactant, reduces the thickness of the liquid film, and reduces the mass transfer resistance;
  • the circulation unit 6 which is connected to the reactor and the micro-interface generator, is used to adjust the temperature of the reactants in the reactor, provide entrainment power for the micro-interface generator, and provide The reaction material circulates along the inside of the catalyst holder to outside the catalyst holder to provide circulation power, so that the reactants and the catalyst are in full contact.
  • the micro-interface generator includes:
  • the first micro-interface generator 51 is a pneumatic micro-interface generator, the first micro-interface generator is located in the fully mixed flow reaction zone in the reactor, and the first micro-interface generator is used to break propylene into micrometers. After the crushing is completed, the micron-scale bubbles are output to the fully mixed flow reaction zone in the reactor, and the deionized water in the fully mixed flow reaction zone in the reactor is mixed to form a gas-liquid emulsion;
  • the second micro-interface generator 52 is a hydraulic micro-interface generator, the second micro-interface generator is located in the reflux reaction zone in the reactor, and the second micro-interface generator is used for crushing and entraining the
  • the unreacted propylene in the upper part of the reflux reaction zone in the reactor forms micron-scale micron-scale bubbles, mixes the micron-scale bubbles with deionized water to form a gas-liquid emulsion, and outputs the gas-liquid emulsion to the fully mixed flow reaction zone to interact with
  • the gas-liquid emulsion output by the first micro-interface generator is offset so that unreacted propylene participates in the reaction again.
  • the inner and outer side walls of the catalyst placer are made of stainless steel wire mesh.
  • the second micro-interface generator is located inside the catalyst placer.
  • the first propylene transmission pipe 7, the propylene transmission main pipe 8 and the deionized water transmission pipe 9 are arranged in the fully mixed flow reaction zone, and the first pump body 10 is installed on the propylene transmission main pipe.
  • the two ends of the first propylene transmission pipe are respectively connected with the first micro-interface generator and the propylene transmission header, and the first pump body is used to transmit propylene along the propylene transmission header and the first propylene transmission pipe
  • a third pump body 11 is installed on the deionized water transfer tube, and the third pump body feeds deionized water into the reactor along the deionized water transfer tube .
  • the second propylene transmission pipe 12, the return pipe 13, and the tail gas discharge pipe 14 are provided in the reflux reaction zone; both ends of the second propylene transmission pipe are connected to the propylene transmission main pipe and The second micro-interface generator is connected; one end of the reflux tube is connected with the third micro-interface generator, the other end of the reflux tube is located on the upper part of the reflux reaction zone, and the reflux tube is used to transfer unreacted Propylene to the second micro-interface generator; the tail gas discharge pipe is used to discharge the tail gas in the reactor.
  • the circulation unit includes a heat exchanger 61 and a second pump body 62.
  • the second pump body is used to pump the products in the reactor into the heat exchanger for heat exchange.
  • the product is discharged, the entrainment power is provided for the second micro-interface generator, and the circulating power is provided for the reaction material in the reactor to circulate from the inside of the catalyst holder to the outside of the catalyst holder, so that the reactants and Full contact of the catalyst.
  • the catalyst is a phosphoric acid diatomaceous earth catalyst, and the phosphoric acid loading amount of the catalyst is 20% to 30% by weight.
  • the present invention provides a submerged propylene hydration micro-interface strengthening reaction process, including:
  • Step 1 Working by the third pump body, transfer deionized water to the reactor along the deionized water transfer pipe;
  • Step 2 Through the work of the first pump body, propylene is transferred to the first micro-interface generator along the propylene transfer manifold and the first propylene transfer pipe, and at the same time along the propylene transfer manifold and the first micro-interface generator.
  • the two propylene transmission pipe is transmitted to the second micro-interface generator;
  • Step 3 The first micro-interface generator works to break the propylene into micron-sized micro-sized bubbles and output the micro-sized bubbles to the fully mixed flow reaction zone in the reactor and the reactor after the crushing is completed.
  • the deionized water in the fully mixed flow reaction zone is mixed to form a gas-liquid emulsion;
  • the second micro-interface generator works to break and entrain the unreacted propylene in the upper part of the reflux reaction zone in the reactor to form micron-scale micron-scale bubbles, Mix the micron-sized bubbles with deionized water to form a gas-liquid emulsion and output the gas-liquid emulsion to the fully mixed flow reaction zone to counteract the gas-liquid emulsion output from the first micro-interface generator to make unreacted
  • the propylene in the reactor again participates in the reaction;
  • the gas-liquid emulsion of propylene and deionized water in the reactor is in contact with the catalyst holder and reacts to produce isopropano
  • Step 4 In step 3, the remaining tail gas in the reactor is discharged along the tail gas exhaust pipe for subsequent tail gas treatment;
  • Step 5 In step 3, with the production of isopropanol, the circulation unit operates to exchange heat treatment for the product, adjust the temperature of the reactants in the reactor, provide entrainment power for the micro-interface generator, and The reaction materials in the reactor are circulated from the inside of the catalyst holder to outside the catalyst holder to provide circulating power.
  • the temperature in the reactor is 170-180°C, and the pressure is 1.7-2.0Mpa.
  • the temperature of the reactor is 170°C, and the pressure inside the reactor is 1.7Mpa;
  • the gas-liquid ratio in the first micro-interface generator is 800:1;
  • the gas-liquid ratio in the second micro-interface generator is 3:1000;
  • the single-pass conversion rate of propylene is 26% after using the system and process.
  • the temperature of the reactor is 175°C, and the pressure inside the reactor is 1.8Mpa;
  • the gas-liquid ratio in the first micro-interface generator is 800:1;
  • the gas-liquid ratio in the second micro-interface generator is 3:1000
  • the single-pass conversion rate of propylene is 26% after using the system and process.
  • the temperature of the reactor is 176°C, and the pressure inside the reactor is 1.9Mpa;
  • the gas-liquid ratio in the first micro-interface generator is 800:1;
  • the gas-liquid ratio in the second micro-interface generator is 3:1000;
  • the single-pass conversion rate of propylene is 26% after using the system and process.
  • the temperature of the reactor is 178°C, and the pressure inside the reactor is 2.0Mpa;
  • the gas-liquid ratio in the first micro-interface generator is 800:1;
  • the gas-liquid ratio in the second micro-interface generator is 3:1000;
  • the temperature of the reactor is 180°C, and the pressure inside the reactor is 2.0Mpa;
  • the gas-liquid ratio in the first micro-interface generator is 800:1;
  • the gas-liquid ratio in the second micro-interface generator is 3:1000;

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Abstract

本发明涉及一种浸没式丙烯水合微界面强化反应系统及工艺，包括：反应器、第一微界面发生器和第二微界面发生器等。本发明通过微界面发生器破碎丙烯使其形成微米尺度的微米级气泡与反应物去离子水混合形成气液乳化物，以增大气液两相的相界面积，并达到在较低预设操作条件范围内强化传质的效果；同时，微米级气泡能够与去离子水充分混合形成气液乳化物，通过将气液两相充分混合，能够保证系统中的去离子水与丙烯充分接触，同时两者与催化剂充分接触，有效提高制备异丙醇的效率。

Description

一种浸没式丙烯水合微界面强化反应系统及工艺 技术领域
本发明涉及异丙醇制备技术领域，尤其涉及一种浸没式丙烯水合微界面强化反应系统及工艺。
背景技术
烯烃可通过水合变为相应的醇，常用的方法主要有间接水合法和直接水合法，其中间接水合法需要将烯烃进行酯化和水解，此反应以浓硫酸作为介质，浓硫酸消耗量巨大，废液处理量大，对设备腐蚀严重，因此新工业生产装置基本不再采用此方法。
异丙醇为无色透明挥发性液体，可与水混溶，也可溶于醇、醚、苯、氯仿等，对树脂、橡胶等有机物与无机物有溶解性，具有乙醇、丙酮等有机物相似的气味。异丙醇有着广泛的工业用途，可以作为化工原料生产异丙醚、丙酮、过氧化氢等，也可以作为高效的溶剂，提取天然物质中有效成分，被广泛应用于医药生产等行业，同时还可以作为调和汽油的添加剂、清洁剂、脱水剂、防冻剂等，也可用作护肤品，应用于化妆品行业。
气相直接水合法最早由德国维巴公司所开发，现有气相直接水合法生产异丙醇工艺过程为液态丙烯、去离子水和循环丙烯气体一起通入反应器，反应温度180～260℃，反应压力2～2.5Mpa，丙烯气体在催化剂作用下与去离子水反应生成异丙醇，后反应产物经水洗精馏等流程进行精制即可。
该工艺对环境污染小，相对于间接水合法工艺流程更为简单而被广泛应用，但该方法在使用过程中存在明显缺点与不足：
在丙烯气体和去离子水接触过程中，气液两项混合，产生较大较多气泡，由于气泡较多较大，致使气液两项无法充分混合，并且影响与催化剂的接触，降低制备异丙醇的效率，丙烯单程转化率只有6％～7％。
发明内容
为此，本发明提供一种浸没式丙烯水合微界面强化反应系统及工艺，用以提 高现有技术中制备异丙醇的效率。
一方面，本发明提供一种浸没式丙烯水合微界面强化反应系统，包括：
反应器，用以为去离子水和丙烯提供反应场所制备异丙醇，所述反应器内设置有催化剂放置器，所述催化剂放置器呈圆柱环状且与所述反应器同轴，所述催化剂放置器的内外侧壁上分别均匀设置有小孔，所述催化剂放置器的上下端面由环状盲板封闭，所述催化剂放置器的空腔内装载有催化剂，所述催化剂放置器浸没于反应物中，所述反应器由全混流反应区和回流反应区组成；所述全混流反应区，其设置在所述反应器的下方，用以装载去离子水、丙烯和催化剂并为丙烯水合反应提供反应空间；所述回流反应区，其设置在所述反应器的上方，用以将未反应的丙烯进行回流处理并使未反应的丙烯与去离子水再次进行反应；
微界面发生器，其将气体的压力能和/或液体的动能转变为气泡表面能并传递给气体反应物，将气体反应物丙烯破碎形成直径≥1μm、且＜1mm的微米级气泡，以提高气体反应物与液体反应物之间的传质面积、减小液膜厚度、降低传质阻力；
循环单元，其与所述反应器和所述微界面发生器相连通，用以调节所述反应器内反应物温度、为所述微界面发生器提供卷吸动力以及为所述反应器内的反应物料沿所述催化剂放置器内循环至所述催化剂放置器外提供循环动力，以使反应物与催化剂的充分接触。
进一步的，所述微界面发生器包括：
第一微界面发生器，其为气动式微界面发生器，所述第一微界面发生器位于所述反应器内的全混流反应区，所述第一微界面发生器用以将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内的全混流反应区与所述反应器内的全混流反应区内的去离子水混合形成气液乳化物；
第二微界面发生器，其为液动式微界面发生器，所述第二微界面发生器位于所述反应器内的回流反应区，所述第二微界面发生器用以破碎卷吸所述反应器内的回流反应区上部未反应的丙烯形成微米尺度的微米级气泡，将微米级气泡与去离子水混合形成气液乳化物并将气液乳化物输出至所述全混流反应区以与所述第一微界面发生器输出的气液乳化物进行对冲，使未反应的丙烯再次参与反应。
进一步的，所述催化剂放置器的内外侧壁由不锈钢丝网构成。
进一步的，所述第二微界面发生器位于所述催化剂放置器内部。
进一步的，所述全混流反应区内设置有第一丙烯传输管、丙烯传输总管和去离子水传输管，所述丙烯传输总管上安装有第一泵体，所述第一丙烯传输管的两端分别与所述第一微界面发生器和丙烯传输总管相连接，所述第一泵体用以将丙烯沿所述丙烯传输总管和所述第一丙烯传输管传输至所述第一微界面发生器；所述去离子水传输管上安装有第三泵体，所述第三泵体将去离子水沿所述去离子水传输管输入所述反应器内。
进一步的，所述回流反应区内设置有第二丙烯传输管、回流管、尾气排出管；所述第二丙烯传输管的两端分别与所述丙烯传输总管和所述第二微界面发生器相连接；所述回流管的一端与所述第三微界面发生器相连接，所述回流管的另一端位于所述回流反应区上部，所述回流管用以传递未反应的丙烯至所述第二微界面发生器；所述尾气排出管用于排出所述反应器内的尾气。
进一步的，所述循环单元包括换热器和第二泵体，所述第二泵体用以将所述反应器内产物抽出至所述换热器内进行换热后将产物排出、为所述第二微界面发生器提供卷吸动力以及为所述反应器内的反应物料沿所述催化剂放置器内循环至所述催化剂放置器外提供循环动力，以使反应物与催化剂的充分接触。
另一方面，本发明提供一种浸没式丙烯水合微界面强化反应工艺，包括：
步骤1：通过所述第三泵体工作，将去离子沿所述去离子水传输管传输至所述反应器内；
步骤2：通过所述第一泵体工作，将丙烯沿所述丙烯传输总管和所述第一丙烯传输管传输至所述第一微界面发生器，同时沿所述丙烯传输总管和所述第二丙烯传输管传输至所述第二微界面发生器；
步骤3：所述第一微界面发生器工作将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内的全混流反应区与所述反应器内的全混流反应区内的去离子水混合形成气液乳化物；所述第二微界面发生器工作破碎卷吸所述反应器内的回流反应区上部未反应的丙烯形成微米尺度的微米级气泡，将微米级气泡与去离子水混合形成气液乳化物并将气液乳化物输出至所述全混流反应区以与所述第一微界面发生器输出的气液乳化物进行对冲，使未反应的丙烯再次参与反应；所述反应器内丙烯和去离子水的气液乳化物均与所述 催化剂放置器接触并反应生成异丙醇；
步骤4：步骤3中所述反应器内剩余尾气沿所述尾气排气管排出，进行后续尾气处理；
步骤5：步骤3中，随异丙醇的生成，所述循环单元工作，对产物进行换热处理，调节所述反应器内反应物温度、为所述微界面发生器提供卷吸动力以及为所述反应器内的反应物料沿所述催化剂放置器内循环至所述催化剂放置器外提供循环动力。
进一步的，所述反应器内的温度为170～180℃，压力为1.7～2.0Mpa。
与现有技术相比，本发明的有益效果在于，本发明通过破碎丙烯气体使其形成微米尺度的微米级气泡，微米级气泡具备常规气泡所不具备的理化性质，由球体体积及表面积的计算公式可知，在总体积不变的情况下，气泡的总表面积与单个气泡直径成反比，由此可知微米级气泡的总表面积巨大，使微米级气泡与去离子水混合形成气液乳化物，以增大气液两相的接触面积，并达到在较低预设操作条件范围内强化传质的效果，有效提高制备异丙醇的转化率和效率；
进一步的，反应器，用以为去离子水和丙烯提供反应场所制备异丙醇，所述反应器内设置有催化剂放置器，所述催化剂放置器呈圆柱环状且与所述反应器同轴，所述催化剂放置器的内外侧壁上分别均匀设置有小孔，所述催化剂放置器的上下端面由环状盲板封闭，所述催化剂放置器的空腔内装载有催化剂，所述催化剂放置器浸没于反应物中，所述反应器由全混流反应区和回流反应区组成；所述全混流反应区，其设置在所述反应器的下方，用以装载去离子水、丙烯和催化剂并为丙烯水合反应提供反应空间；所述回流反应区，其设置在所述反应器的上方，用以将未反应的丙烯进行回流处理并使未反应的丙烯与去离子水再次进行反应；
微界面发生器，其将气体的压力能和/或液体的动能转变为气泡表面能并传递给气体反应物，将气体反应物丙烯破碎形成直径≥1μm、且＜1mm的微米级气泡，以提高气体反应物与液体反应物之间的传质面积、减小液膜厚度、降低传质阻力；
循环单元，其与所述反应器和所述微界面发生器相连通，用以调节所述反应器内反应物温度、为所述微界面发生器提供卷吸动力以及为所述反应器内的反应物料沿所述催化剂放置器内循环至所述催化剂放置器外提供循环动力，以使反应 物与催化剂的充分接触。
进一步的，所述微界面发生器包括：
第一微界面发生器，其为气动式微界面发生器，所述第一微界面发生器位于所述反应器内的全混流反应区，所述第一微界面发生器用以将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内的全混流反应区与所述反应器内的全混流反应区内的去离子水混合形成气液乳化物；
第二微界面发生器，其为液动式微界面发生器，所述第二微界面发生器位于所述反应器内的回流反应区，所述第二微界面发生器用以破碎卷吸所述反应器内的回流反应区上部未反应的丙烯形成微米尺度的微米级气泡，将微米级气泡与去离子水混合形成气液乳化物并将气液乳化物输出至所述全混流反应区以与所述第一微界面发生器输出的气液乳化物进行对冲，使未反应的丙烯再次参与反应。所述反应器内丙烯和去离子水的气液乳化物均与所述催化剂放置器充分接触，进一步提高丙烯单程转化率。
进一步的，所述催化剂放置器的内外侧壁由不锈钢丝网构成。圆筒形所述催化剂放置器的内外侧均可裸露出催化剂，使得所述反应器内丙烯和去离子水的气液乳化物均与所述催化剂放置器充分接触，进一步提高丙烯单程转化率。
进一步的，所述第二微界面发生器位于所述催化剂放置器内部。
进一步的，所述全混流反应区内设置有第一丙烯传输管、丙烯传输总管和去离子水传输管，所述丙烯传输总管上安装有第一泵体，所述第一丙烯传输管的两端分别与所述第一微界面发生器和丙烯传输总管相连接，所述第一泵体用以将丙烯沿所述丙烯传输总管和所述第一丙烯传输管传输至所述第一微界面发生器；所述去离子水传输管上安装有第三泵体，所述第三泵体将去离子水沿所述去离子水传输管输入所述反应器内。
进一步的，所述回流反应区内设置有第二丙烯传输管、回流管、尾气排出管；所述第二丙烯传输管的两端分别与所述丙烯传输总管和所述第二微界面发生器相连接；所述回流管的一端与所述第三微界面发生器相连接，所述回流管的另一端位于所述回流反应区上部，所述回流管用以传递未反应的丙烯至所述第二微界面发生器；所述尾气排出管用于排出所述反应器内的尾气。
进一步的，所述循环单元包括换热器和第二泵体，所述第二泵体用以将所述 反应器内产物抽出至所述换热器内进行换热后将产物排出、为所述第二微界面发生器提供卷吸动力以及为所述反应器内的反应物料沿所述催化剂放置器内循环至所述催化剂放置器外提供循环动力，以使反应物与催化剂的充分接触。
附图说明
图1为本发明所述一种浸没式丙烯水合微界面强化反应系统的结构示意图。
1-反应器、2-催化剂放置器、3-全混流反应区、4-回流反应区、51-第一微界面发生器、52-第二微界面发生器、6-循环单元、61-换热器、62-第二泵体、7-第一丙烯传输管、8-丙烯传输总管、9-去离子水传输管、10-第一泵体、11-第三泵体、12-第二丙烯传输管、13-回流管、14-尾气排出管。
具体实施方式
下面参照附图来描述本发明的优选实施方式。本领域技术人员应当理解的是，这些实施方式仅仅用于解释本发明的技术原理，并非在限制本发明的保护范围。
需要说明的是，在本发明的描述中，术语“上”、“下”、“左”、“右”、“内”、“外”等指示的方向或位置关系的术语是基于附图所示的方向或位置关系，这仅仅是为了便于描述，而不是指示或暗示所述装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本发明的限制。
此外，还需要说明的是，在本发明的描述中，除非另有明确的规定和限定，术语“安装”、“相连”、“连接”应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或一体地连接；可以是机械连接，也可以是电连接；可以是直接相连，也可以通过中间媒介间接相连，可以是两个元件内部的连通。对于本领域技术人员而言，可根据具体情况理解上述术语在本发明中的具体含义。
请参阅图1所示，其为本发明提供一种浸没式丙烯水合微界面强化反应系统，包括：
反应器1，用以为去离子水和丙烯提供反应场所制备异丙醇，所述反应器内设置有催化剂放置器2，所述催化剂放置器呈圆柱环状且与所述反应器同轴，所述催化剂放置器的内外侧壁上分别均匀设置有小孔，所述催化剂放置器的上下端面由环状盲板封闭，所述催化剂放置器的空腔内装载有催化剂，所述催化剂放置 器浸没于反应物中，所述反应器由全混流反应区3和回流反应区4组成；所述全混流反应区，其设置在所述反应器的下方，用以装载去离子水、丙烯和催化剂并为丙烯水合反应提供反应空间；所述回流反应区，其设置在所述反应器的上方，用以将未反应的丙烯进行回流处理并使未反应的丙烯与去离子水再次进行反应；
微界面发生器，其将气体的压力能和/或液体的动能转变为气泡表面能并传递给气体反应物，将气体反应物丙烯破碎形成直径≥1μm、且＜1mm的微米级气泡，以提高气体反应物与液体反应物之间的传质面积、减小液膜厚度、降低传质阻力；
循环单元6，其与所述反应器和所述微界面发生器相连通，用以调节所述反应器内反应物温度、为所述微界面发生器提供卷吸动力以及为所述反应器内的反应物料沿所述催化剂放置器内循环至所述催化剂放置器外提供循环动力，以使反应物与催化剂的充分接触。
请继续参阅图1，所述微界面发生器包括：
第一微界面发生器51，其为气动式微界面发生器，所述第一微界面发生器位于所述反应器内的全混流反应区，所述第一微界面发生器用以将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内的全混流反应区与所述反应器内的全混流反应区内的去离子水混合形成气液乳化物；
第二微界面发生器52，其为液动式微界面发生器，所述第二微界面发生器位于所述反应器内的回流反应区，所述第二微界面发生器用以破碎卷吸所述反应器内的回流反应区上部未反应的丙烯形成微米尺度的微米级气泡，将微米级气泡与去离子水混合形成气液乳化物并将气液乳化物输出至所述全混流反应区以与所述第一微界面发生器输出的气液乳化物进行对冲，使未反应的丙烯再次参与反应。
请继续参阅图1，所述催化剂放置器的内外侧壁由不锈钢丝网构成。
请继续参阅图1，所述第二微界面发生器位于所述催化剂放置器内部。
请继续参阅图1，所述全混流反应区内设置有第一丙烯传输管7、丙烯传输总管8和去离子水传输管9，所述丙烯传输总管上安装有第一泵体10，所述第一丙烯传输管的两端分别与所述第一微界面发生器和丙烯传输总管相连接，所述第一泵体用以将丙烯沿所述丙烯传输总管和所述第一丙烯传输管传输至所述第一 微界面发生器；所述去离子水传输管上安装有第三泵体11，所述第三泵体将去离子水沿所述去离子水传输管输入所述反应器内。
请继续参阅图1，所述回流反应区内设置有第二丙烯传输管12、回流管13、尾气排出管14；所述第二丙烯传输管的两端分别与所述丙烯传输总管和所述第二微界面发生器相连接；所述回流管的一端与所述第三微界面发生器相连接，所述回流管的另一端位于所述回流反应区上部，所述回流管用以传递未反应的丙烯至所述第二微界面发生器；所述尾气排出管用于排出所述反应器内的尾气。
请继续参阅图1，所述循环单元包括换热器61和第二泵体62，所述第二泵体用以将所述反应器内产物抽出至所述换热器内进行换热后将产物排出、为所述第二微界面发生器提供卷吸动力以及为所述反应器内的反应物料沿所述催化剂放置器内循环至所述催化剂放置器外提供循环动力，以使反应物与催化剂的充分接触。
请继续参阅图1，所述催化剂为磷酸硅藻土催化剂，所述催化剂的磷酸负载量为20wt％～30wt％。
请继续参阅图1，本发明提供一种浸没式丙烯水合微界面强化反应工艺，包括：
步骤1：通过所述第三泵体工作，将去离子沿所述去离子水传输管传输至所述反应器内；
步骤2：通过所述第一泵体工作，将丙烯沿所述丙烯传输总管和所述第一丙烯传输管传输至所述第一微界面发生器，同时沿所述丙烯传输总管和所述第二丙烯传输管传输至所述第二微界面发生器；
步骤3：所述第一微界面发生器工作将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内的全混流反应区与所述反应器内的全混流反应区内的去离子水混合形成气液乳化物；所述第二微界面发生器工作破碎卷吸所述反应器内的回流反应区上部未反应的丙烯形成微米尺度的微米级气泡，将微米级气泡与去离子水混合形成气液乳化物并将气液乳化物输出至所述全混流反应区以与所述第一微界面发生器输出的气液乳化物进行对冲，使未反应的丙烯再次参与反应；所述反应器内丙烯和去离子水的气液乳化物均与所述催化剂放置器接触并反应生成异丙醇；
步骤4：步骤3中所述反应器内剩余尾气沿所述尾气排气管排出，进行后续尾气处理；
步骤5：步骤3中，随异丙醇的生成，所述循环单元工作，对产物进行换热处理，调节所述反应器内反应物温度、为所述微界面发生器提供卷吸动力以及为所述反应器内的反应物料沿所述催化剂放置器内循环至所述催化剂放置器外提供循环动力。
进一步的，所述反应器内的温度为170～180℃，压力为1.7～2.0Mpa。
实施例1
使用上述系统及工艺进行异丙醇制备，其中：
所述反应器温度为170℃，所述反应器内压强为1.7Mpa；
所述第一微界面发生器内的气液比为800：1；
所述第二微界面发生器内的气液比为3:1000；
经检测，使用所述系统及工艺后，丙烯单程转化率为26％。
实施例2
使用上述系统及工艺进行异丙醇制备，其中：
所述反应器温度为175℃，所述反应器内压强为1.8Mpa；
所述第一微界面发生器内的气液比为800：1；
所述第二微界面发生器内的气液比为3:1000
经检测，使用所述系统及工艺后，丙烯单程转化率为26％。
实施例3
使用上述系统及工艺进行异丙醇制备，其中：
所述反应器温度为176℃，所述反应器内压强为1.9Mpa；
所述第一微界面发生器内的气液比为800：1；
所述第二微界面发生器内的气液比为3:1000；
经检测，使用所述系统及工艺后，丙烯单程转化率为26％。
实施例4
使用上述系统及工艺进行异丙醇制备，其中：
所述反应器温度为178℃，所述反应器内压强为2.0Mpa；
所述第一微界面发生器内的气液比为800：1；
所述第二微界面发生器内的气液比为3:1000；
经检测，使用所述系统及工艺后，丙烯单程转化率为27％。
实施例5
使用上述系统及工艺进行异丙醇制备，其中：
所述反应器温度为180℃，所述反应器内压强为2.0Mpa；
所述第一微界面发生器内的气液比为800：1；
所述第二微界面发生器内的气液比为3:1000；
经检测，使用所述系统及工艺后，丙烯单程转化率为27％。
对比例
使用现有技术丙烯直接水合法进行异丙醇制备，其中，本对比例选用的工艺参数与所述实施例5中的工艺参数相同。
经检测，丙烯单程转化率为6％。
至此，已经结合附图所示的优选实施方式描述了本发明的技术方案，但是，本领域技术人员容易理解的是，本发明的保护范围显然不局限于这些具体实施方式。在不偏离本发明的原理的前提下，本领域技术人员可以对相关技术特征做出等同的更改或替换，这些更改或替换之后的技术方案都将落入本发明的保护范围之内。
以上所述仅为本发明的优选实施例，并不用于限制本发明；对于本领域的技术人员来说，本发明可以有各种更改和变化。凡在本发明的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本发明的保护范围之内。

Claims (9)

  1. 一种浸没式丙烯水合微界面强化反应系统，其特征在于，包括：
    反应器，用以为去离子水和丙烯提供反应场所制备异丙醇，所述反应器内设置有催化剂放置器，所述催化剂放置器呈圆柱环状且与所述反应器同轴，所述催化剂放置器的内外侧壁上分别均匀设置有小孔，所述催化剂放置器的上下端面由环状盲板封闭，所述催化剂放置器的空腔内装载有催化剂，所述催化剂放置器浸没于反应物中，所述反应器由全混流反应区和回流反应区组成；所述全混流反应区，其设置在所述反应器的下方，用以装载去离子水、丙烯和催化剂并为丙烯水合反应提供反应空间；所述回流反应区，其设置在所述反应器的上方，用以将未反应的丙烯进行回流处理并使未反应的丙烯与去离子水再次进行反应；
    微界面发生器，其将气体的压力能和/或液体的动能转变为气泡表面能并传递给气体反应物，将气体反应物丙烯破碎形成直径≥1μm、且＜1mm的微米级气泡，以提高气体反应物与液体反应物之间的传质面积、减小液膜厚度、降低传质阻力；
    循环单元，其与所述反应器和所述微界面发生器相连通，用以调节所述反应器内反应物温度、为所述微界面发生器提供卷吸动力以及为所述反应器内的反应物料沿所述催化剂放置器内循环至所述催化剂放置器外提供循环动力，以使反应物与催化剂的充分接触。
  2. 根据权利要求1所述的一种浸没式丙烯水合微界面强化反应系统，其特征在于，所述微界面发生器包括：
    第一微界面发生器，其为气动式微界面发生器，所述第一微界面发生器位于所述反应器内的全混流反应区，所述第一微界面发生器用以将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内的全混流反应区与所述反应器内的全混流反应区内的去离子水混合形成气液乳化物；
    第二微界面发生器，其为液动式微界面发生器，所述第二微界面发生器位于所述反应器内的回流反应区，所述第二微界面发生器用以破碎卷吸所述反应器内的回流反应区上部未反应的丙烯形成微米尺度的微米级气泡，将微米级气泡与去离子水混合形成气液乳化物并将气液乳化物输出至所述全混流反应区以与所述第一微界面发生器输出的气液乳化物进行对冲，使未反应的丙烯再次参与反应。
  3. 根据权利要求2所述的一种浸没式丙烯水合微界面强化反应系统，其特 征在于，所述催化剂放置器的内外侧壁由不锈钢丝网构成。
  4. 根据权利要求3所述的一种浸没式丙烯水合微界面强化反应系统，其特征在于，所述第二微界面发生器位于所述催化剂放置器内部。
  5. 根据权利要求2所述的一种浸没式丙烯水合微界面强化反应系统，其特征在于，所述全混流反应区内设置有第一丙烯传输管、丙烯传输总管和去离子水传输管，所述丙烯传输总管上安装有第一泵体，所述第一丙烯传输管的两端分别与所述第一微界面发生器和丙烯传输总管相连接，所述第一泵体用以将丙烯沿所述丙烯传输总管和所述第一丙烯传输管传输至所述第一微界面发生器；所述去离子水传输管上安装有第三泵体，所述第三泵体将去离子水沿所述去离子水传输管输入所述反应器内。
  6. 根据权利要求2所述的一种浸没式丙烯水合微界面强化反应系统，其特征在于，所述回流反应区内设置有第二丙烯传输管、回流管、尾气排出管；所述第二丙烯传输管的两端分别与所述丙烯传输总管和所述第二微界面发生器相连接；所述回流管的一端与所述第三微界面发生器相连接，所述回流管的另一端位于所述回流反应区上部，所述回流管用以传递未反应的丙烯至所述第二微界面发生器；所述尾气排出管用于排出所述反应器内的尾气。
  7. 根据权利要求6所述的一种浸没式丙烯水合微界面强化反应系统，其特征在于，所述循环单元包括换热器和第二泵体，所述第二泵体用以将所述反应器内产物抽出至所述换热器内进行换热后将产物排出、为所述第二微界面发生器提供卷吸动力以及为所述反应器内的反应物料沿所述催化剂放置器内循环至所述催化剂放置器外提供循环动力，以使反应物与催化剂的充分接触。
  8. 一种浸没式丙烯水合微界面强化反应工艺，其特征在于，包括：
    步骤1：通过所述第三泵体工作，将去离子沿所述去离子水传输管传输至所述反应器内；
    步骤2：通过所述第一泵体工作，将丙烯沿所述丙烯传输总管和所述第一丙烯传输管传输至所述第一微界面发生器，同时沿所述丙烯传输总管和所述第二丙烯传输管传输至所述第二微界面发生器；
    步骤3：所述第一微界面发生器工作将丙烯破碎形成微米尺度的微米级气泡并在破碎完成后将微米级气泡输出至所述反应器内的全混流反应区与所述反应 器内的全混流反应区内的去离子水混合形成气液乳化物；所述第二微界面发生器工作破碎卷吸所述反应器内的回流反应区上部未反应的丙烯形成微米尺度的微米级气泡，将微米级气泡与去离子水混合形成气液乳化物并将气液乳化物输出至所述全混流反应区以与所述第一微界面发生器输出的气液乳化物进行对冲，使未反应的丙烯再次参与反应，所述反应器内丙烯和去离子水的气液乳化物均与所述催化剂放置器接触并反应生成异丙醇；
    步骤4：步骤3中所述反应器内剩余尾气沿所述尾气排气管排出，进行后续尾气处理；
    步骤5：步骤3中，随异丙醇的生成，所述循环单元工作，对产物进行换热处理，调节所述反应器内反应物温度、为所述微界面发生器提供卷吸动力以及为所述反应器内的反应物料沿所述催化剂放置器内循环至所述催化剂放置器外提供循环动力。
  9. 根据权利要求9所述的一种浸没式丙烯水合微界面强化反应工艺，其特征在于，所述反应器内的温度为170～180℃，压力为1.7～2.0Mpa。
PCT/CN2020/092755 2020-03-25 2020-05-28 一种浸没式丙烯水合微界面强化反应系统及工艺 WO2021189638A1 (zh)

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