CN111569784A - Sectional type intensified reaction system and process for preparing isopropanol by propylene hydration - Google Patents
Sectional type intensified reaction system and process for preparing isopropanol by propylene hydration Download PDFInfo
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- CN111569784A CN111569784A CN202010217972.1A CN202010217972A CN111569784A CN 111569784 A CN111569784 A CN 111569784A CN 202010217972 A CN202010217972 A CN 202010217972A CN 111569784 A CN111569784 A CN 111569784A
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- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 title claims abstract description 110
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 96
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 96
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 95
- 238000006703 hydration reaction Methods 0.000 title claims abstract description 33
- 230000036571 hydration Effects 0.000 title claims abstract description 22
- 238000004519 manufacturing process Methods 0.000 title abstract description 13
- 239000007788 liquid Substances 0.000 claims abstract description 64
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 56
- 239000008367 deionised water Substances 0.000 claims abstract description 55
- 229910021641 deionized water Inorganic materials 0.000 claims abstract description 55
- 239000000839 emulsion Substances 0.000 claims abstract description 35
- 239000000376 reactant Substances 0.000 claims abstract description 28
- 239000003054 catalyst Substances 0.000 claims abstract description 14
- 238000000746 purification Methods 0.000 claims abstract description 13
- 238000012546 transfer Methods 0.000 claims abstract description 11
- 238000004821 distillation Methods 0.000 claims description 38
- 239000007791 liquid phase Substances 0.000 claims description 38
- 239000000463 material Substances 0.000 claims description 37
- 239000007921 spray Substances 0.000 claims description 35
- 239000012043 crude product Substances 0.000 claims description 34
- 239000012071 phase Substances 0.000 claims description 30
- 238000005507 spraying Methods 0.000 claims description 20
- 239000000047 product Substances 0.000 claims description 11
- 239000012141 concentrate Substances 0.000 claims description 7
- 238000004891 communication Methods 0.000 claims description 6
- 238000011010 flushing procedure Methods 0.000 claims description 4
- 238000011068 loading method Methods 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 3
- 239000011344 liquid material Substances 0.000 claims 2
- 230000000694 effects Effects 0.000 abstract description 3
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- 238000002360 preparation method Methods 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical group OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
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- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
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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
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1487—Removing organic compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
- B01D53/185—Liquid distributors
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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
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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
- B01J8/0278—Feeding reactive fluids
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- 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
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- 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
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- 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
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
Abstract
The invention relates to a sectional type intensified reaction system and a process for preparing isopropanol by propylene hydration, which comprises the following steps: a reactor, a micro-interface generator, a purification unit, etc. According to the invention, the micro-interface generator is used for crushing propylene to form micron-scale bubbles, and the micron-scale bubbles are mixed with the reactant deionized water to form a gas-liquid emulsion, so that the phase interface area of gas-liquid two phases is increased, and the effect of strengthening mass transfer within a lower preset operation condition range is achieved; meanwhile, the micron-sized bubbles can be fully mixed with deionized water to form a gas-liquid emulsion, the gas-liquid two phases are fully mixed, the deionized water and propylene in the system can be ensured to be fully contacted, and meanwhile, the micron-sized bubbles and the deionized water are fully contacted with a catalyst, so that the efficiency of preparing the isopropanol is effectively improved.
Description
Technical Field
The invention relates to the technical field of isopropanol preparation, in particular to a sectional type intensified reaction system and a process for preparing isopropanol by propylene hydration.
Background
The demand of the isopropanol market in China is increased year by year, but the supply increase of the isopropanol is obviously laggard behind the market demand, China is a large country for importing the isopropanol, a large amount of isopropanol is imported from abroad for a long time, the production of the isopropanol in China starts to start late, the process research on the isopropanol is developed from the last 60 th century, a Lanzhou petrochemical refinery has once established a device for producing the isopropanol by indirect hydration, 600 ten thousand tons of isopropanol are produced every year, but the process is laggard behind, the cost is high, and the production is forced to stop because of no market competitiveness;
at present, the industrial production method of isopropanol mainly comprises a propylene indirect hydration method and a propylene direct hydration method, wherein the propylene indirect hydration method has low requirement on the purity of propylene gas and high conversion rate of propylene, but the method has complex process, a large amount of water vapor is needed in the reaction process, sulfuric acid has corrosion effect on equipment, and the environmental pollution is serious, so the method is gradually replaced by the direct hydration method.
The propylene gas-phase direct hydration method is firstly developed by the German Viba company, the existing gas-phase direct hydration method for producing the isopropanol comprises the steps of introducing liquid propylene, deionized water and circulating propylene gas into a reactor together, wherein the reaction temperature is 180-260 ℃, the reaction pressure is 2-2.5 Mpa, and the propylene gas reacts with the deionized water under the action of a catalyst to generate the isopropanol.
The process has little pollution to the environment, is simpler and widely applied compared with the process flow of an indirect hydration method, but has obvious defects and shortcomings in the using process:
in the contact process of propylene gas and deionized water, the gas and the liquid are mixed to generate larger bubbles, and the gas and the liquid cannot be fully mixed due to the larger bubbles, so that the contact with a catalyst is influenced, the preparation efficiency of isopropanol is reduced, and the conversion per pass of propylene is only 6-7%.
Disclosure of Invention
Therefore, the invention provides a sectional type intensified reaction system and a sectional type intensified reaction process for preparing isopropanol by propylene hydration, which are used for improving the conversion rate and efficiency of preparing the isopropanol in the prior art.
In one aspect, the present invention provides an intensified reaction system for preparing isopropanol by sectional hydration of propylene, comprising:
the reactor is used for providing reaction sites for deionized water and propylene to prepare isopropanol, and a first section reaction zone and a second section reaction zone are arranged in the reactor; the first-stage reaction zone is arranged below the reactor and used for loading deionized water, propylene and a catalyst and providing a reaction space for propylene hydration reaction; the second-stage reaction zone is arranged above the reactor and is used for carrying out reflux treatment on the unreacted propylene and enabling the unreacted propylene to react with the deionized water again;
the micro-interface generator converts the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of bubbles and transmits the surface energy to a gas reactant, and the propylene of the gas reactant is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm, so that the mass transfer area between the gas reactant and the liquid reactant is increased, the thickness of a liquid film is reduced, and the mass transfer resistance is reduced;
the circulating unit is communicated with the reactor and the micro-interface generator and used for adjusting the temperature of reactants in the reactor and providing entrainment power for the micro-interface generator, and an interception net is arranged between the circulating unit and the reactor and used for intercepting the catalyst;
the condenser is communicated with the reactor and is used for separating and treating products, and an interception net is arranged between the condenser and the reactor and is used for intercepting the catalyst;
a purification unit in communication with the condenser for purifying the product.
Further, the micro-interface generator includes:
the first micro-interface generator is a pneumatic micro-interface generator, is positioned in a first-stage reaction zone in the reactor, and is used for crushing propylene to form micron-scale micro-bubbles and outputting the micron-scale micro-bubbles to the first-stage reaction zone in the reactor after the crushing is finished to be mixed with deionized water in the first-stage reaction zone in the reactor to form a gas-liquid emulsion;
and the second micro-interface generator is a hydraulic micro-interface generator, is positioned in a second section of reaction zone in the reactor, is used for crushing and entrainment of unreacted propylene on the upper part of the second section of reaction zone in the reactor to form micron-scale micron-sized bubbles, mixes the micron-scale bubbles with deionized water to form a gas-liquid emulsion, and outputs the gas-liquid emulsion to the first section of reaction zone so as to carry out counter flushing with the gas-liquid emulsion output by the first micro-interface generator, so that the unreacted propylene participates in the reaction again.
Furthermore, the circulating unit comprises a first heat exchanger and a first pump body, and the first pump body is used for pumping the materials in the reactor out to the first heat exchanger for heat exchange and then circulating the materials back to the second micro-interface generator and providing entrainment power for the second micro-interface generator.
Furthermore, the feed end of the condenser is communicated with the discharge end of the reactor, the discharge end of the condenser is communicated with the purification unit, and the condenser is used for condensing the crude product discharged from the reactor, so that the crude product is divided into a gas-phase crude product and a liquid-phase crude product.
Further, the purification unit includes spray column and distillation column, the discharge end of spray column with the liquid phase feed end of distillation column is linked together, the discharge end of condenser includes gaseous phase discharge end and liquid phase discharge end, the gaseous phase discharge end of condenser with the spray column is linked together, the liquid phase discharge end of condenser with the distillation column is linked together.
Furthermore, deionized water is introduced into a spraying device in the spraying tower, the deionized water is sprayed out from top to bottom in the spraying tower through the spraying device and is contacted with the gas-phase material, isopropanol in the gas-phase material is recycled into the deionized water, and propylene tail gas overflowing from the top of the spraying tower is pressurized and transmitted to the first micro-interface generator through a circulating compressor.
Furthermore, a multi-stage tower plate is arranged in the distillation tower, a second heat exchanger and a second pump body are arranged on the side portion of the distillation tower, liquid-phase materials entering the distillation tower move from top to bottom along the multi-stage tower plate, and the second pump body concentrates the liquid-phase materials by moving steam subjected to heat exchange through the second heat exchanger from bottom to top along the multi-stage tower plate in the distillation tower.
In another aspect, the present invention provides a staged propylene hydration process for producing isopropanol by an enhanced reaction, comprising:
step 1: adding deionized water into the reactor;
step 2: introducing propylene into the first micro-interface generator, wherein the first micro-interface generator is used for crushing the propylene to form micron-scale micron-sized bubbles, outputting the micron-scale bubbles to a first-stage reaction zone in the reactor after the micron-scale bubbles are crushed, mixing the micron-scale bubbles with deionized water in the first-stage reaction zone in the reactor to form a gas-liquid emulsion, and contacting the gas-liquid emulsion with a catalyst to generate a propylene hydration reaction;
and step 3: the second micro-interface generator works to crush and suck unreacted propylene at the upper part of a second section of reaction zone in the reactor to form micron-scale micron-sized bubbles, the micron-sized bubbles are mixed with deionized water to form a gas-liquid emulsion, and the gas-liquid emulsion is output to the first section of reaction zone to be flushed with the gas-liquid emulsion output by the first micro-interface generator, so that the unreacted propylene participates in the reaction again;
and 4, step 4: the circulating unit works to regulate the temperature of reactants in the reactor, the materials in the reactor are pumped out to the first heat exchanger through the work of the first pump body to be cooled, and then the materials are circulated back to the second micro-interface generator, and meanwhile entrainment power is provided for the second micro-interface generator;
and 5: the crude product generated in the step 3 enters a condenser, the condenser enables the crude product to be divided into a gas-phase crude product and a liquid-phase crude product, the gas-phase crude product enters a spray tower, a spray device in the spray tower sprays deionized water in the spray tower from top to bottom and contacts with a gas-phase material, isopropanol in the gas-phase material is recycled into the deionized water to form a liquid-phase isopropanol solution, and propylene tail gas overflowing from the top of the spray tower is pressurized and transmitted to a first micro-interface generator through a circulating compressor and circularly participates in a propylene hydration reaction;
step 6: and 5, allowing the liquid-phase crude product and the liquid-phase isopropanol solution in the spray tower to enter the distillation tower and move from top to bottom along the multi-stage tower plates, allowing the second pump body to move the steam subjected to heat exchange by the second heat exchanger from bottom to top along the multi-stage tower plates in the distillation tower to concentrate the liquid-phase material, and discharging the concentrated product isopropanol along the bottom of the distillation tower.
Further, the temperature of the reactor is 160-240 ℃, and the pressure is 1.6-2.0 Mpa.
Compared with the prior art, the method has the beneficial effects that the propylene gas is crushed to form micron-sized bubbles with micron scale, the micron-sized bubbles have physicochemical properties which are not possessed by conventional bubbles, and the calculation formula of the volume and the surface area of the sphere can know that the total surface area of the bubbles is inversely proportional to the diameter of a single bubble under the condition of unchanged total volume, so that the total surface area of the micron-sized bubbles is huge, the micron-sized bubbles and deionized water are mixed to form gas-liquid emulsion, the contact area of gas and liquid phases is increased, the effect of strengthening mass transfer within a lower preset operation condition range is achieved, and the efficiency of preparing isopropanol is effectively improved;
further, the reactor is used for providing a reaction site for deionized water and propylene to prepare isopropanol, and a first-stage reaction zone and a second-stage reaction zone are arranged in the reactor; the first-stage reaction zone is arranged below the reactor and used for loading deionized water, propylene and a catalyst and providing a reaction space for propylene hydration reaction; the second-stage reaction zone is arranged above the reactor and is used for carrying out reflux treatment on the unreacted propylene and enabling the unreacted propylene to react with the deionized water again;
the micro-interface generator converts pressure energy of gas and/or kinetic energy of liquid into surface energy of bubbles and transmits the surface energy of the bubbles to a gas reactant, the gas reactant is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm so as to improve the mass transfer area between the gas reactant and the liquid reactant, reduce the thickness of a liquid film and reduce mass transfer resistance, and the crushed micron-sized bubbles of the liquid reactant and the gas reactant are mixed to form a gas-liquid emulsion so as to strengthen the mass transfer efficiency and the reaction efficiency between the liquid reactant and the gas reactant within a preset operating condition range;
the circulating unit is communicated with the reactor and the micro-interface generator and is used for adjusting the temperature of reactants in the reactor and providing entrainment power for the micro-interface generator;
the condenser is communicated with the reactor and is used for separating and treating products;
a purification unit in communication with the condenser for purifying the product.
Further, the micro-interface generator includes:
the first micro-interface generator is a pneumatic micro-interface generator, is positioned in a first-stage reaction zone in the reactor, and is used for crushing propylene to form micron-scale micro-bubbles and outputting the micron-scale micro-bubbles to the first-stage reaction zone in the reactor after the crushing is finished to be mixed with deionized water in the first-stage reaction zone in the reactor to form a gas-liquid emulsion;
and the second micro-interface generator is a hydraulic micro-interface generator, is positioned in a second section of reaction zone in the reactor, is used for crushing and entrainment of unreacted propylene on the upper part of the second section of reaction zone in the reactor to form micron-scale micron-sized bubbles, mixes the micron-scale bubbles with deionized water to form a gas-liquid emulsion, and outputs the gas-liquid emulsion to the first section of reaction zone so as to carry out counter flushing with the gas-liquid emulsion output by the first micro-interface generator, so that the unreacted propylene participates in the reaction again.
Furthermore, the circulating unit comprises a first heat exchanger and a first pump body, and the first pump body is used for pumping the materials in the reactor out to the first heat exchanger for cooling and then circulating the materials back to the second micro-interface generator, and providing entrainment power for the second micro-interface generator.
Furthermore, the feed end of the condenser is communicated with the discharge end of the reactor, the discharge end of the condenser is communicated with the purification unit, and the condenser is used for condensing the crude product discharged from the reactor, so that the crude product is divided into a gas-phase crude product and a liquid-phase crude product.
Further, the purification unit includes spray column and distillation column, the discharge end of spray column with the liquid phase feed end of distillation column is linked together, the discharge end of condenser includes gaseous phase discharge end and liquid phase discharge end, the gaseous phase discharge end of condenser with the spray column is linked together, the liquid phase discharge end of condenser with the distillation column is linked together.
Furthermore, deionized water is introduced into a spraying device in the spraying tower, the deionized water is sprayed out from top to bottom in the spraying tower through the spraying device and is contacted with the gas-phase material, isopropanol in the gas-phase material is recycled into the deionized water, and propylene tail gas overflowing from the top of the spraying tower is pressurized and transmitted to the first micro-interface generator through a circulating compressor. The propylene is recycled to participate in the propylene hydration reaction, and the raw materials are saved to a certain extent.
Furthermore, a multi-stage tower plate is arranged in the distillation tower, a second heat exchanger and a second pump body are arranged on the side portion of the distillation tower, liquid-phase materials entering the distillation tower move from top to bottom along the multi-stage tower plate, and the second pump body concentrates the liquid-phase materials by moving steam subjected to heat exchange through the second heat exchanger from bottom to top along the multi-stage tower plate in the distillation tower.
Drawings
FIG. 1 is a schematic structural diagram of an enhanced reaction system for preparing isopropanol by sectional hydration of propylene according to the present invention.
The method comprises the following steps of 1-a reactor, 2-a first stage reaction zone, 3-a second stage reaction zone, 41-a first micro-interface generator, 42-a second micro-interface generator, 5-a first heat exchanger, 6-a first pump body, 7-a condenser, 8-a spray tower, 9-a distillation tower, 10-a circulating compressor, 11-a second heat exchanger and 12-a second pump body.
Detailed Description
Preferred embodiments of the present invention are described below with reference to the accompanying drawings. It should be understood by those skilled in the art that these embodiments are only for explaining the technical principle of the present invention, and do not limit the scope of the present invention.
It should be noted that in the description of the present invention, the terms of direction or positional relationship indicated by the terms "upper", "lower", "left", "right", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, which are only for convenience of description, and do not indicate or imply that the device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
Furthermore, it should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Referring to fig. 1, the present invention provides an enhanced reaction system for preparing isopropanol by hydration of propylene in a staged manner, comprising:
the reactor 1 is used for providing reaction sites for deionized water and propylene to prepare isopropanol, and a first-stage reaction zone 2 and a second-stage reaction zone 3 are arranged in the reactor; the first-stage reaction zone is arranged below the reactor and used for loading deionized water, propylene and a catalyst and providing a reaction space for propylene hydration reaction; the second-stage reaction zone is arranged above the reactor and is used for carrying out reflux treatment on the unreacted propylene and enabling the unreacted propylene to react with the deionized water again;
the micro-interface generator converts the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of bubbles and transmits the surface energy to a gas reactant, and the propylene of the gas reactant is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm, so that the mass transfer area between the gas reactant and the liquid reactant is increased, the thickness of a liquid film is reduced, and the mass transfer resistance is reduced;
the circulating unit is communicated with the reactor and the micro-interface generator and is used for adjusting the temperature of reactants in the reactor and providing entrainment power for the micro-interface generator;
the condenser 7 is communicated with the reactor and is used for separating and treating products;
a purification unit in communication with the condenser for purifying the product.
With continued reference to fig. 1, the micro-interface generator includes:
the first micro-interface generator 41 is a pneumatic micro-interface generator, and is located in a first-stage reaction zone in the reactor, and is configured to crush propylene to form micron-sized bubbles, and output the micron-sized bubbles to the first-stage reaction zone in the reactor after crushing is completed, and mix the micron-sized bubbles with deionized water in the first-stage reaction zone in the reactor to form a gas-liquid emulsion;
and the second micro-interface generator 42 is a hydraulic micro-interface generator, is positioned in a second section of reaction zone in the reactor, is used for crushing and entrainment of unreacted propylene on the upper part of the second section of reaction zone in the reactor to form 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 first section of reaction zone so as to carry out counter flushing with the gas-liquid emulsion output by the first micro-interface generator, so that the unreacted propylene participates in the reaction again.
With reference to fig. 1, the circulation unit includes a first heat exchanger 5 and a first pump body 6, and the first pump body is configured to pump the material in the reactor into the first heat exchanger for heat exchange, and then circulate the material back to the second micro interface generator, and provide entrainment power for the second micro interface generator.
With continued reference to fig. 1, the feed end of the condenser is in communication with the discharge end of the reactor, the discharge end of the condenser is in communication with the purification unit, and the condenser is configured to condense the crude product discharged from the reactor, such that the crude product is separated into a gas-phase crude product and a liquid-phase crude product.
With continued reference to fig. 1, the purification unit includes a spray tower 8 and a distillation tower 9, the discharge end of the spray tower is communicated with the liquid phase feed end of the distillation tower, the discharge end of the condenser includes a gas phase discharge end and a liquid phase discharge end, the gas phase discharge end of the condenser is communicated with the spray tower, and the liquid phase discharge end of the condenser is communicated with the distillation tower.
Referring to fig. 1, deionized water is introduced into the spraying device in the spraying tower, the deionized water is sprayed out from top to bottom in the spraying tower through the spraying device and contacts with the gas-phase material, isopropanol in the gas-phase material is recovered into the deionized water, and propylene tail gas overflowing from the top of the spraying tower is pressurized and transmitted to the first micro-interface generator through the circulating compressor 10.
Referring to fig. 1, a plurality of stages of tower plates are arranged in the distillation tower, a second heat exchanger 11 and a second pump body 12 are arranged on the side of the distillation tower, the liquid-phase material entering the distillation tower moves from top to bottom along the plurality of stages of tower plates, and the second pump body concentrates the liquid-phase material by moving the steam after heat exchange by the second heat exchanger from bottom to top along the plurality of stages of tower plates in the distillation tower.
The catalyst is a phosphoric acid diatomite catalyst.
With continued reference to FIG. 1, the present invention provides a staged propylene hydration enhanced isopropanol production process, comprising:
step 1: adding deionized water into the reactor;
step 2: introducing propylene into the first micro-interface generator, wherein the first micro-interface generator is used for crushing the propylene to form micron-scale micron-sized bubbles, outputting the micron-scale bubbles to a first-stage reaction zone in the reactor after the micron-scale bubbles are crushed, mixing the micron-scale bubbles with deionized water in the first-stage reaction zone in the reactor to form a gas-liquid emulsion, and contacting the gas-liquid emulsion with a catalyst to generate a propylene hydration reaction;
and step 3: the second micro-interface generator works to crush and suck unreacted propylene at the upper part of a second section of reaction zone in the reactor to form micron-scale micron-sized bubbles, the micron-sized bubbles are mixed with deionized water to form a gas-liquid emulsion, and the gas-liquid emulsion is output to the first section of reaction zone to be flushed with the gas-liquid emulsion output by the first micro-interface generator, so that the unreacted propylene participates in the reaction again;
and 4, step 4: the circulating unit works to regulate the temperature of reactants in the reactor, the materials in the reactor are pumped out to the first heat exchanger through the work of the first pump body to be cooled, and then the materials are circulated back to the second micro-interface generator, and meanwhile entrainment power is provided for the second micro-interface generator;
and 5: the crude product generated in the step 3 enters a condenser, the condenser enables the crude product to be divided into a gas-phase crude product and a liquid-phase crude product, the gas-phase crude product enters a spray tower, a spray device in the spray tower sprays deionized water in the spray tower from top to bottom and contacts with a gas-phase material, isopropanol in the gas-phase material is recycled into the deionized water to form a liquid-phase isopropanol solution, and propylene tail gas overflowing from the top of the spray tower is pressurized and transmitted to a first micro-interface generator through a circulating compressor and circularly participates in a propylene hydration reaction;
step 6: and 5, allowing the liquid-phase crude product and the liquid-phase isopropanol solution in the spray tower to enter the distillation tower and move from top to bottom along the multi-stage tower plates, allowing the second pump body to move the steam subjected to heat exchange by the second heat exchanger from bottom to top along the multi-stage tower plates in the distillation tower to concentrate the liquid-phase material, and discharging the concentrated product isopropanol along the bottom of the distillation tower.
The temperature of the reactor is 160-240 ℃, and the pressure is 1.6-2.0 Mpa.
Example 1
Isopropanol production was carried out using the above system and process, wherein:
the temperature of the reactor is 160 ℃, and the pressure in the reactor is 1.6 Mpa;
the gas-liquid ratio in the first micro-interface generator is 900: 1;
the gas-liquid ratio in the second micro-interface generator is 3: 1000;
after the system and the process are used, the once-through conversion rate of the propylene is 25 percent.
Example 2
Isopropanol production was carried out using the above system and process, wherein:
the temperature of the reactor is 170 ℃, and the pressure in the reactor is 1.7 Mpa;
the gas-liquid ratio in the first micro-interface generator is 900: 1;
the gas-liquid ratio in the second micro-interface generator is 3:1000
After the system and the process are used, the once-through conversion rate of the propylene is 25 percent.
Example 3
Isopropanol production was carried out using the above system and process, wherein:
the temperature of the reactor is 180 ℃, and the pressure in the reactor is 1.8 Mpa;
the gas-liquid ratio in the first micro-interface generator is 900: 1;
the gas-liquid ratio in the second micro-interface generator is 3: 1000;
after the system and the process are used, the once-through conversion rate of the propylene is 27 percent.
Example 4
Isopropanol production was carried out using the above system and process, wherein:
the temperature of the reactor is 190 ℃, and the pressure in the reactor is 1.9 Mpa;
the gas-liquid ratio in the first micro-interface generator is 900: 1;
the gas-liquid ratio in the second micro-interface generator is 3: 1000;
after the system and the process are used, the once-through conversion rate of the propylene is 26 percent.
Example 5
Isopropanol production was carried out using the above system and process, wherein:
the temperature of the reactor is 200 ℃, and the pressure in the reactor is 2.0 Mpa;
the gas-liquid ratio in the first micro-interface generator is 900: 1;
the gas-liquid ratio in the second micro-interface generator is 3: 1000;
after the system and the process are used, the once-through conversion rate of the propylene is 27 percent.
Comparative example
The isopropanol preparation was carried out using a prior art propylene direct hydration process, wherein the process parameters selected for this comparative example were the same as those described in example 5.
The detection proves that the conversion per pass of the propylene is 5.8 percent.
So far, the technical solutions of the present invention have been described in connection with the preferred embodiments shown in the drawings, but it is easily understood by those skilled in the art that the scope of the present invention is obviously not limited to these specific embodiments. Equivalent changes or substitutions of related technical features can be made by those skilled in the art without departing from the principle of the invention, and the technical scheme after the changes or substitutions can fall into the protection scope of the invention.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention; various modifications and alterations to this invention will become apparent to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (9)
1. An intensified reaction system for preparing isopropanol by sectional propylene hydration, which is characterized by comprising:
the reactor is used for providing reaction sites for deionized water and propylene to prepare isopropanol, and a first section reaction zone and a second section reaction zone are arranged in the reactor; the first-stage reaction zone is arranged below the reactor and used for loading deionized water, propylene and a catalyst and providing a reaction space for propylene hydration reaction; the second-stage reaction zone is arranged above the reactor and is used for carrying out reflux treatment on the unreacted propylene and enabling the unreacted propylene to react with the deionized water again;
the micro-interface generator converts the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of bubbles and transmits the surface energy to a gas reactant, and the propylene of the gas reactant is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm, so that the mass transfer area between the gas reactant and the liquid reactant is increased, the thickness of a liquid film is reduced, and the mass transfer resistance is reduced;
the circulating unit is communicated with the reactor and the micro-interface generator and is used for adjusting the temperature of reactants in the reactor and providing entrainment power for the micro-interface generator;
the condenser is communicated with the reactor and is used for separating and treating products;
a purification unit in communication with the condenser for purifying the product.
2. The system of claim 1, wherein the micro-interface generator comprises:
the first micro-interface generator is a pneumatic micro-interface generator, is positioned in a first-stage reaction zone in the reactor, and is used for crushing propylene to form micron-scale bubbles and outputting the micron-scale bubbles to the first-stage reaction zone in the reactor after crushing is finished to be mixed with deionized water in the first-stage reaction zone in the reactor to form a gas-liquid emulsion;
and the second micro-interface generator is a hydraulic micro-interface generator, is positioned in a second section of reaction zone in the reactor, is used for crushing and entrainment of unreacted propylene on the upper part of the second section of reaction zone in the reactor to form micron-scale micron-sized bubbles, mixes the micron-scale bubbles with deionized water to form a gas-liquid emulsion, and outputs the gas-liquid emulsion to the first section of reaction zone so as to carry out counter flushing with the gas-liquid emulsion output by the first micro-interface generator, so that the unreacted propylene participates in the reaction again.
3. The system of claim 2, wherein the circulation unit comprises a first heat exchanger and a first pump body, and the first pump body is used for pumping the materials in the reactor into the first heat exchanger for heat exchange, then circulating the materials back to the second micro-interface generator, and providing entrainment power for the second micro-interface generator.
4. The system of claim 2, wherein the feed end of the condenser is connected to the discharge end of the reactor, the discharge end of the condenser is connected to the purification unit, and the condenser is used to condense the crude product discharged from the reactor, so that the crude product is separated into a gas-phase crude product and a liquid-phase crude product.
5. The system of claim 4, wherein the purification unit comprises a spray tower and a distillation tower, the discharge end of the spray tower is communicated with the liquid-phase feed end of the distillation tower, the discharge end of the condenser comprises a gas-phase discharge end and a liquid-phase discharge end, the gas-phase discharge end of the condenser is communicated with the spray tower, and the liquid-phase discharge end of the condenser is communicated with the distillation tower.
6. The system of claim 5, wherein deionized water is introduced into a spraying device in the spraying tower, the spraying device sprays the deionized water from top to bottom in the spraying tower and contacts with the gas-phase material, the isopropanol in the gas-phase material is recovered into the deionized water, and the propylene tail gas overflowing from the top of the spraying tower is pressurized and transmitted to the first micro-interface generator through a circulating compressor.
7. The system as claimed in claim 5, wherein the distillation tower is internally provided with a plurality of stages of trays, the side part of the distillation tower is provided with a second heat exchanger and a second pump body, the liquid material entering the distillation tower moves from top to bottom along the plurality of stages of trays, and the second pump body concentrates the liquid material by moving the steam after heat exchange by the second heat exchanger from bottom to top along the plurality of stages of trays in the distillation tower.
8. A sectional type intensified reaction process for preparing isopropanol by propylene hydration is characterized by comprising the following steps:
step 1: adding deionized water into the reactor;
step 2: introducing propylene into the first micro-interface generator, wherein the first micro-interface generator is used for crushing the propylene to form micron-scale micron-sized bubbles, outputting the micron-scale bubbles to a first-stage reaction zone in the reactor after the micron-scale bubbles are crushed, mixing the micron-scale bubbles with deionized water in the first-stage reaction zone in the reactor to form a gas-liquid emulsion, and contacting the gas-liquid emulsion with a catalyst to generate a propylene hydration reaction;
and step 3: the second micro-interface generator works to crush and suck unreacted propylene at the upper part of a second section of reaction zone in the reactor to form micron-scale micron-sized bubbles, the micron-sized bubbles are mixed with deionized water to form a gas-liquid emulsion, and the gas-liquid emulsion is output to the first section of reaction zone to be flushed with the gas-liquid emulsion output by the first micro-interface generator, so that the unreacted propylene participates in the reaction again;
and 4, step 4: the circulating unit works to regulate the temperature of reactants in the reactor, the materials in the reactor are pumped out to the first heat exchanger through the work of the first pump body to be cooled, and then the materials are circulated back to the second micro-interface generator, and meanwhile entrainment power is provided for the second micro-interface generator;
and 5: the crude product generated in the step 3 enters a condenser, the condenser enables the crude product to be divided into a gas-phase crude product and a liquid-phase crude product, the gas-phase crude product enters a spray tower, a spray device in the spray tower sprays deionized water in the spray tower from top to bottom and contacts with a gas-phase material, isopropanol in the gas-phase material is recycled into the deionized water to form a liquid-phase isopropanol solution, and propylene tail gas overflowing from the top of the spray tower is pressurized and transmitted to a first micro-interface generator through a circulating compressor and circularly participates in a propylene hydration reaction;
step 6: and 5, allowing the liquid-phase crude product and the liquid-phase isopropanol solution in the spray tower to enter the distillation tower and move from top to bottom along the multi-stage tower plates, allowing the second pump body to move the steam subjected to heat exchange by the second heat exchanger from bottom to top along the multi-stage tower plates in the distillation tower to concentrate the liquid-phase material, and discharging the concentrated product isopropanol along the bottom of the distillation tower.
9. The intensified reaction process for preparing isopropanol by the hydration of sectional propylene as claimed in claim 8, wherein the temperature in the reactor is 160-240 ℃ and the pressure is 1.6-2.0 Mpa.
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