CN111957272A - Polyether polyol production system and process - Google Patents
Polyether polyol production system and process Download PDFInfo
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- CN111957272A CN111957272A CN202010773259.5A CN202010773259A CN111957272A CN 111957272 A CN111957272 A CN 111957272A CN 202010773259 A CN202010773259 A CN 202010773259A CN 111957272 A CN111957272 A CN 111957272A
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- 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
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/10—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by stirrers or by rotary drums or rotary receptacles or endless belts
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- 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
- B01J19/18—Stationary reactors having moving elements inside
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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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
- B01J19/1868—Stationary reactors having moving elements inside resulting in a loop-type movement
- B01J19/1881—Stationary reactors having moving elements inside resulting in a loop-type movement externally, i.e. the mixture leaving the vessel and subsequently re-entering it
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
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- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
- C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
- C08G65/26—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds
- C08G65/2603—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing oxygen
- C08G65/2606—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing oxygen containing hydroxyl groups
- C08G65/2609—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing oxygen containing hydroxyl groups containing aliphatic hydroxyl groups
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Abstract
The invention provides a polyether polyol production system and a process, wherein the polyether polyol production system comprises a reaction kettle, a jet reactor and an external circulation cooler; the jet reactor is arranged at the top of the reaction kettle and is communicated with the space in the reaction kettle; the gas phase inlet of the injection reactor is communicated with the gas outlet at the top of the reaction kettle; the feed inlet of the injection reactor is communicated with the outlet of the mixer; the mixer is provided with at least one feeding hole; the outer circulation cooler is independently arranged outside the reaction kettle, a liquid inlet of the outer circulation cooler is communicated with one liquid outlet of the reaction kettle, and a liquid outlet of the outer circulation cooler is communicated with a liquid inlet of the injection reactor. The polyether polyol production system provided by the invention adopts the upward-spraying loop injection reactor, so that the reaction speed can be increased, the feeding speed can be increased, the curing time can be shortened, and the unit-time productivity can be improved.
Description
Technical Field
The invention belongs to the field of chemical synthesis, and particularly relates to a polyether polyol production system and a polyether polyol production process.
Background
Polyether polyols are important raw materials for the polyurethane industry. The application fields of polyurethane products are quite wide, and the polyurethane products can be used for interior parts of automobiles, trains, ships, airplanes and the like, mattresses, sofas, chairs, bedding, carpets, building energy-saving heat-insulating materials, sealing materials and waterproof materials. The polyurethane product is used for the heat insulating material of household appliances such as refrigerator, electric appliance shell, insulating device, package, and synthetic fiber, namely spandex, which can be used for manufacturing high-grade sportswear, diving suit and the like.
At present, the traditional polyether polyol production process is a strong base catalysis process, a batch reactor is adopted, and after a catalyst and an initiator are added, a propylene oxide monomer and an ethylene oxide monomer are added for polymerization reaction. Because of the reaction temperature, the propylene oxide and ethylene oxide monomer can be vaporized and can not be fully contacted with an initiator and a catalyst, the reaction rate is low, the curing time is long, the content of vent gas monomer is high after the reaction, and the reaction heat is removed by adopting an inner coil pipe, so that the feeding speed is limited, and the yield is also limited.
The venturi jet reactor has been developed in recent decades for gas-liquid two-phase reactions. The principle is that high-speed mobile phase passes through a Venturi nozzle to form local negative pressure, other phases are sucked in and fully mixed, and then the phases are uniformly distributed in a reactor to complete the reaction. The reaction of polyether polyols is a gas-liquid phase reaction and a jet reactor may be used to overcome the problems in the reaction.
The problem mainly to be solved for increasing the polymerization rate of polyether polyol is to enhance the mixing effect of propylene oxide and ethylene oxide with a catalyst and an initiator, and the two phases can be fully mixed to realize the full contact of reaction materials for reaction; the reaction heat is effectively and quickly removed, the removal rate of the reaction heat determines the feeding rate of the propylene oxide and the ethylene oxide, and the quick removal of the reaction heat can realize high-speed feeding and high yield in unit time; the monomer which is not fully contacted and reacted in the gas phase space at the top of the reaction kettle is effectively mixed with the reaction liquid, the gas phase space at the top of the reaction kettle contains a large amount of micromolecule monomer and propylene oxide, the traditional process adopts stirring to mix the monomer and the reaction liquid, the unreacted material in the part of space cannot be contacted with the catalyst, long curing time is needed, the monomer and the catalyst in the part of space slowly react through diffusion on the liquid level, and the curing time can be effectively shortened.
Traditional venturi sprays reactor and all uses the mixed gaseous phase of mobile phase to form highly dispersed mixed phase, realizes quick reaction, has solved the problem of the mixed effect of oxygen propane, ethylene oxide and catalyst, initiator, but polyether production process is the high exothermic reaction, if unable effectual removal reaction heat, can lead to the reaction overtemperature, the unqualified scheduling problem of product to can not solve the curing time problem.
The polyether reaction of the traditional external circulation cooler only adopts reaction mixed liquid to be cooled through the external circulation cooler and then returns to the reaction kettle through the nozzle, and the reaction is continued in the kettle, so that the problems that reaction heat is removed and the effect of enhancing two-phase contact by an auxiliary stirrer is solved, the influence on the reaction rate is not obvious, and the reaction efficiency is low are still caused are solved.
Disclosure of Invention
In view of this, the present invention provides a polyether polyol production system, which overcomes the defects of the prior art, and adopts an upward-spraying loop injection reactor, so as to accelerate the reaction rate, increase the feeding speed, shorten the curing time, and increase the productivity per unit time.
In order to achieve the purpose, the technical scheme of the invention is realized as follows:
a polyether polyol production system comprises a reaction kettle, a jet reactor and an external circulation cooler;
the reaction kettle is provided with at least one feeding hole, at least one air outlet and at least one liquid outlet;
the jet reactor is arranged at the top of the reaction kettle and is communicated with the space in the reaction kettle; the gas phase inlet of the injection reactor is communicated with the gas outlet at the top of the reaction kettle; the feed inlet of the injection reactor is communicated with the outlet of the mixer; the mixer is provided with at least one feeding hole;
the outer circulation cooler is independently arranged outside the reaction kettle, a liquid inlet of the outer circulation cooler is communicated with one liquid outlet of the reaction kettle, and a liquid outlet of the outer circulation cooler is communicated with a liquid inlet of the injection reactor.
Furthermore, a liquid inlet of the external circulation cooler is communicated with a liquid outlet at the bottom of the reaction kettle through a pipeline, and an external circulation pump is arranged on the pipeline.
Furthermore, the external circulating pump adopts a centrifugal pump, and the flow of the centrifugal pump can realize a circulation ratio of 1-20.
Further, the external circulation cooler adopts a fixed tube plate type heat exchanger or a U-shaped tube heat exchanger.
Further, a stirrer is arranged in the reaction kettle.
Furthermore, the inner surface and the outer surface of the reaction kettle are both provided with a steam heating coil and a circulating water cooling coil.
Further, the injection reactor is a venturi injection reactor.
Further, the jet reactor comprises an air suction chamber, a mixing reaction chamber and a diffuser which are sequentially communicated from top to bottom; a plurality of nozzles are arranged in the air suction chamber; the lower end of the mixing reaction chamber and the diffuser extend into the reaction kettle, the upper part of the upper end of the mixing reaction chamber and the air suction chamber are positioned outside the reaction kettle, and the air suction chamber is provided with a gas phase inlet of the injection reactor, a feed inlet of the injection reactor and a liquid inlet of the injection reactor; the diffuser is horn-shaped, and the lower end and the upper end of the diffuser form an obtuse angle.
Another object of the present invention is to provide a process for producing polyether polyol using the polyether polyol production system as described above, to produce polyether polyol.
In order to achieve the purpose, the technical scheme of the invention is realized as follows:
a process for producing polyether polyol by using the polyether polyol production system comprises the steps of introducing polyether, a catalyst and an initiator in a reaction kettle as an external circulation liquid into a jet reactor, mixing and reacting the external circulation liquid with gas phase and raw materials from the top of the reaction kettle in a mixing reaction chamber of the jet reactor, and then spraying a reaction product into the reaction kettle through a diffuser; the raw material is a mixture of propylene oxide and ethylene oxide or propylene oxide.
Preferably, the gas phase at the top of the reactor is unreacted monomer comprising propylene oxide and oligomers of small molecules thereof.
Further preferably, the polyether polyol production process comprises the following steps:
1) adding a catalyst and an initiator into the reaction kettle, heating to a reaction temperature, and starting an external circulating pump with a circulation ratio of 1-20;
2) sucking the gas phase at the top of the reaction kettle and the raw material gas phase into the injection reactor, then fully mixing and reacting the gas phase and the external circulation liquid in the mixing reaction chamber, and then spraying the reaction product into the reaction kettle through a diffuser;
3) after the reaction feeding is finished, continuously keeping the starting of the external circulating pump, fully contacting the gas phase at the top of the reaction kettle with the mixed solution for reaction, and stopping the external circulation until the pressure at the top of the reaction kettle is reduced to normal pressure;
preferably, the catalyst is potassium hydroxide solid or potassium hydroxide solution, the initiator is one or a mixture of more than two of glycerol, propylene glycol, diethylene glycol, sorbitol and the like, the reaction temperature is 80-120 ℃, the reaction pressure is 0-0.4MPa, and the reaction time is 4-12 h.
Preferably, the propylene oxide is used in an amount of 95 to 98 wt% of the total charge.
In the polyether polyol production process, the synthesis principle of the polyether polyol is as follows:
compared with the prior art, the polyether polyol production system has the following advantages:
the polyether polyol production system provided by the invention is additionally provided with the external circulation system and the Venturi injection reactor, so that the polyether polyol can be efficiently produced with minimum change.
The process for producing polyether polyol by using the polyether polyol production system has the following advantages: the large circulation ratio mobile phase can effectively and quickly remove reaction heat, the Venturi jet reactor realizes the full mixing reaction of a catalyst, an initiator, a raw material (can be independent propylene oxide or propylene oxide and ethylene oxide) and unreacted monomers in a gas phase space at the top of the reaction kettle, the problem that the single kettle productivity is difficult to improve in the existing polyether reaction is effectively solved, the contradiction between the removal of the reaction heat and the improvement of the feeding rate is realized, the low investment is realized, the reaction rate is accelerated by small modification, and the energy consumption is saved.
Drawings
FIG. 1 is a schematic diagram showing a simple structure of a polyether polyol production system according to the present invention (which can also be understood as a process flow diagram for polyether polyol production);
FIG. 2 is a schematic diagram of the structure of a spray reactor in the polyether polyol production system of the present invention.
Reference numerals:
1-a reaction kettle; 2-a spray reactor; 201-a suction chamber; 202-a mixing reaction chamber; 203-a diffuser; 204-a nozzle; 205-external circulation liquid inlet; 206-a feed inlet; 207-gas phase inlet; 3-external circulation cooler; 4-a mixer; 5-external circulation pump; 6-a stirrer; 7-a steam heater; 8-the contact position of the reaction kettle end socket and the injection reactor; 9-a catalyst; 10-an initiator; 11-steam; 12-first circulating water; 13-second circulating water; 14-propylene oxide; 15-ethylene oxide; 16-polyether polyol.
Detailed Description
Unless defined otherwise, technical terms used in the following examples have the same meanings as commonly understood by one of ordinary skill in the art to which the present invention belongs. The test reagents used in the following examples, unless otherwise specified, are all conventional biochemical reagents; the experimental methods are conventional methods unless otherwise specified.
The invention is described in detail below with reference to embodiments and the accompanying drawings.
As shown in fig. 1, a polyether polyol production system is characterized in that: comprises a reaction kettle 1, a jet reactor 2 and an external circulation cooler 3; at least one feed inlet, at least one gas outlet and at least one liquid outlet are arranged on the reaction kettle 1. Specifically, according to needs, a feed inlet can be arranged at the top of the reaction kettle 1, all reaction raw materials can be fed into the reaction kettle from the feed inlet, or a plurality of feed inlets can be arranged, and various reaction raw materials can be fed into the reaction kettle from independent feed inlets respectively. As a preferable embodiment, the reaction kettle is provided with two feed inlets at the top, a gas outlet at the top and a liquid outlet at the bottom, wherein the two feed inlets can be used for feeding the catalyst and the initiator respectively, the gas outlet can be used for discharging the gas phase in the reaction kettle during the reaction process, and the liquid outlet is used for discharging the reaction product.
Wherein, the injection reactor 2 is arranged at the top of the reaction kettle 1 and is communicated with the space in the reaction kettle 1. As an alternative embodiment of the invention, the injection reactor 2 is preferably a venturi injection reactor. Further, as shown in fig. 2, the injection reactor 2 includes a suction chamber 201, a mixing reaction chamber 202 and a diffuser 203 which are sequentially communicated from top to bottom; a plurality of nozzles 204 are arranged in the air suction chamber 201; the lower end of the mixing reaction chamber 202 and the diffuser 203 extend into the reaction kettle 1 (the relative installation position of the jet reactor and the reaction kettle is specifically the position marked by the reference numeral 8 in fig. 2), the upper part of the upper end of the mixing reaction chamber 202 and the air suction chamber 201 are positioned outside the reaction kettle 1, and the air suction chamber 201 is provided with a gas phase inlet 207 of the jet reactor 2, a feed inlet 206 of the jet reactor 2 and a liquid inlet (namely, an external circulation liquid inlet 205) of the jet reactor 2; the diffuser 203 is in a horn shape with a small upper end and a large lower end, and the lower end and the upper end of the diffuser form an obtuse angle.
Wherein, the gas phase inlet 207 of the injection reactor 2 is communicated with a gas outlet at the top of the reaction kettle 1; the feed inlet 206 of the injection reactor 2 is communicated with the outlet of the mixer 4, and the mixer 4 is preferably an existing static mixer, so that when propylene oxide and ethylene oxide are used as raw materials, the ethylene oxide and the propylene oxide mixed in the mixer 4 can be introduced into the injection reactor 2 through the feed inlet 206, or when propylene oxide is used as a raw material, the propylene oxide is introduced into the injection reactor 2 through the feed inlet 206 after passing through the mixer. The mixer 4 is provided with at least one feed port, preferably 2 feed ports, one feed port is used for feeding ethylene oxide, and the other feed port is used for feeding propylene oxide, wherein a flow meter and a valve are respectively arranged on pipelines for feeding ethylene oxide and propylene oxide, so that the mixture of ethylene oxide and propylene oxide or the propylene oxide is independently used as the raw material by controlling the opening and closing of the valve according to the requirement.
Wherein, the external circulation cooler 3 is independently arranged outside the reaction kettle 1, a liquid inlet of the external circulation cooler 3 is communicated with a liquid outlet at the bottom of the reaction kettle 1 through a pipeline, and an external circulation pump 5 is arranged on the pipeline; the liquid outlet of the external circulation cooler 3 is communicated with the liquid inlet (namely, the external circulation liquid inlet 205) of the injection reactor 2.
As an alternative embodiment of the invention, the external circulating pump 5 adopts a centrifugal pump, and the flow rate of the centrifugal pump can realize a circulating ratio of 1-20.
As an alternative embodiment of the present invention, the external circulation cooler 3 employs a fixed tube plate heat exchanger or a U-shaped tube heat exchanger, and its cooling medium is selected as second circulating water 13 (it should be noted that the medium is selected as circulating water, but is named as second circulating water 13 in order to distinguish from circulating water in the subsequent evaporation heater 7).
As an optional embodiment of the present invention, in order to stir the reaction raw materials in the reaction kettle, increase the contact of the materials in the reaction, and improve the reaction efficiency, a stirrer 6 is installed in the reaction kettle 1. The stirrer 6 is formed by adopting the conventional stirring equipment in a chemical production reaction kettle, and the structure is not the key point of the invention.
As an optional embodiment of the present invention, in order to ensure a certain reaction temperature, a steam heating coil and a circulating water cooling coil 7 are installed on both the inner surface and the outer surface of the reaction kettle 1. When the temperature needs to be raised, opening the steam 11 and heating to the reaction temperature; the reaction is exothermic, in the reaction process, steam is closed, the first circulating water 12 is opened, the flow of the first circulating water 12 is controlled by the temperature in the reaction kettle, and a certain reaction temperature is kept; after the reaction is finished, the first circulating water 12 is fully opened, and the temperature of the materials is reduced so as to carry out the next operation.
The process for producing polyether polyol by adopting the polyether polyol production system comprises the following steps:
as shown in figure 1, catalyst 9 is added into a reaction kettle 1, different initiators 10 are added according to different quantitative rates of brands, a stirrer 6 is started for mixing, steam of a steam heating coil and a steam heating coil in a circulating water cooling coil 7 is started for heating to 80-120 ℃, the reaction kettle 1 is vacuumized to 1-5KPa (A), an external circulating pump 5 is started, the circulation ratio is 1-20, external circulating liquid returns into the reaction kettle 1 through a spray reactor 2 after passing through an external circulating cooler 3, and high-speed flow of the external circulating liquid passes through a Venturi nozzle 204 to form local negative pressure and can be sucked into gas phase in a gas phase space at the top of the reaction kettle 1. Wherein the catalyst is potassium hydroxide solid or potassium hydroxide solution, and the initiator is one or a mixture of more than two of glycerol, propylene glycol, diethylene glycol, sorbitol and the like. It should be noted that the circulation ratio means the ratio of 1 hour circulation volume to the total volume of the reaction kettle, the circulation ratio is determined, the ratio of the gas phase at the top of the reaction kettle entering the jet reactor, the mixture of propylene oxide and ethylene oxide and the external circulation liquid is determined, in addition, the gas phase at the top of the reaction kettle is the saturated vapor pressure of the substances in the kettle, a part of the substances in the kettle is evaporated until no propylene oxide and micromolecules exist in the kettle, the saturated vapor pressure is reduced to the normal pressure, namely the reaction is finished, and the gas phase has no certain ratio.
The propylene oxide 14 and the ethylene oxide 15 are quantitatively fed according to a preset feeding curve (the feeding curve is known), wherein the feeding amount of the propylene oxide is 1-20t/h, and the feeding amount of the ethylene oxide is 0.1-10 t/h. The propylene oxide and the ethylene oxide are fully mixed by a mixer 5, enter a jet reactor 2, and are fully contacted and mixed with an external circulation liquid in a Venturi jet reactor, the external circulation liquid contains polyether glycol, an initiator and a catalyst, the external circulation liquid rapidly reacts in the Venturi jet reactor and is polymerized, then the external circulation liquid enters a reaction kettle 1 through a nozzle 204, a small part of unreacted monomers (propylene oxide and micromolecule oligomers thereof) enter a top gas phase space of the reaction kettle 1, the pressure in the reaction kettle 1 is gradually increased, the unreacted monomers in the top gas phase space of the reaction kettle are sucked into the Venturi jet reactor by local negative pressure formed by the throat diameter of the Venturi jet reactor, the reaction is continued, and the pressure in the reaction kettle can be kept between 0 and 0.4MPa (G). The heat released by the reaction is removed through an external circulation system, and the external circulation liquid is cooled through an external circulation heat exchanger 3 and then returns to the Venturi jet reactor for continuous reaction. The external circulation cooler 3 adjusts the quantity of circulating water through a reaction kettle temperature control system (the reaction kettle temperature control system is a common temperature adjusting loop, a thermometer and an adjusting valve), and keeps the temperature of the reaction kettle between 80 ℃ and 120 ℃. And after the feeding is finished, the external circulation system continues to work, unreacted monomers in the gas phase space at the top of the reaction kettle are continuously sucked into the venturi injection reactor through the venturi injection reactor for reaction, finally the pressure of the reaction kettle is reduced to normal pressure, the reaction is finished, and the polyether glycol 16 is collected from the bottom of the reaction kettle. In the above process, if only propylene oxide is used as the raw material, the valve on the ethylene oxide feed line can be closed, and other processes are the same.
Taking the case that the raw material is only propylene oxide as an example, the polyether polyols in the examples and the comparative examples are produced by adopting the process, the selection of the specific production formula composition and the reaction conditions is shown in table 1, and the detection results and the process effects of the products in the examples and the comparative examples are shown in table 2.
TABLE 1 formulation composition and reaction conditions selection for polyether polyol production in examples and comparative examples
Remarking: the catalyst examples and comparative examples in table 1 are both KOH solids.
Table 2 results of product testing and process effects in examples and comparative examples
The comparison shows that after the external circulation part and the jet reactor are added, the single-kettle batch time is reduced by about 1/3 compared with the original single-kettle batch time, the propylene oxide feeding speed can be increased by 1/4, the curing time is reduced by half, and the unit time capacity is increased by about 1/3, so that the whole reaction rate and the feeding speed are both increased, the curing time is shortened, and the unit time capacity is increased.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and should not be taken as limiting the invention, so that any modifications, equivalents, improvements and the like, which are within the spirit and principle of the present invention, should be included in the scope of the present invention.
Claims (10)
1. A polyether polyol production system characterized by: comprises a reaction kettle, a jet reactor and an external circulation cooler;
the reaction kettle is provided with at least one feeding hole, at least one air outlet and at least one liquid outlet;
the jet reactor is arranged at the top of the reaction kettle and is communicated with the space in the reaction kettle; the gas phase inlet of the injection reactor is communicated with the gas outlet at the top of the reaction kettle; the feed inlet of the injection reactor is communicated with the outlet of the mixer; the mixer is provided with at least one feeding hole;
the outer circulation cooler is independently arranged outside the reaction kettle, a liquid inlet of the outer circulation cooler is communicated with one liquid outlet of the reaction kettle, and a liquid outlet of the outer circulation cooler is communicated with a liquid inlet of the injection reactor.
2. The polyether polyol production system according to claim 1, characterized in that: the liquid inlet of the external circulation cooler is communicated with the liquid outlet at the bottom of the reaction kettle through a pipeline, and an external circulation pump is arranged on the pipeline.
3. Polyether polyol production system according to claim 2, characterized in that: the external circulating pump adopts a centrifugal pump, and the flow of the centrifugal pump can realize a circulation ratio of 1-20.
4. The polyether polyol production system according to claim 1, characterized in that: the external circulation cooler adopts a fixed tube plate type heat exchanger or a U-shaped tube heat exchanger.
5. The polyether polyol production system according to claim 1, characterized in that: and a stirrer is arranged in the reaction kettle.
6. The polyether polyol production system according to claim 1, characterized in that: and the inner surface and the outer surface of the reaction kettle are both provided with a steam heating coil and a circulating water cooling coil.
7. The polyether polyol production system according to claim 1, characterized in that: the injection reactor is a venturi injection reactor.
8. Polyether polyol production system according to claim 7, characterized in that: the jet reactor comprises an air suction chamber, a mixing reaction chamber and a diffuser which are sequentially communicated from top to bottom; a plurality of nozzles are arranged in the air suction chamber; the lower end of the mixing reaction chamber and the diffuser extend into the reaction kettle, the upper part of the upper end of the mixing reaction chamber and the air suction chamber are positioned outside the reaction kettle, and the air suction chamber is provided with a gas phase inlet of the injection reactor, a feed inlet of the injection reactor and a liquid inlet of the injection reactor; the diffuser is horn-shaped, and the lower end and the upper end of the diffuser form an obtuse angle.
9. A process for producing polyether polyol using the polyether polyol production system according to any one of claims 1 to 8, wherein: introducing polyether, a catalyst and an initiator in a reaction kettle into a jet reactor as an external circulation liquid, mixing and reacting with a gas phase and a raw material from the top of the reaction kettle in a mixing reaction chamber of the jet reactor, and then spraying a reaction product into the reaction kettle through a diffuser; the raw material is a mixture of propylene oxide and ethylene oxide or propylene oxide;
preferably, the gas phase at the top of the reactor is unreacted monomer comprising propylene oxide and oligomers of small molecules thereof.
10. A process for producing polyether polyol according to claim 9, characterized in that: the method comprises the following steps:
1) adding a catalyst and an initiator into the reaction kettle, heating to a reaction temperature, and starting an external circulating pump with a circulation ratio of 1-20;
2) sucking the gas phase at the top of the reaction kettle and the raw material gas phase into the injection reactor, then fully mixing and reacting the gas phase and the external circulation liquid in the mixing reaction chamber, and then spraying the reaction product into the reaction kettle through a diffuser;
3) after the reaction feeding is finished, continuously keeping the starting of the external circulating pump, fully contacting the gas phase at the top of the reaction kettle with the mixed solution for reaction, and stopping the external circulation until the pressure at the top of the reaction kettle is reduced to normal pressure;
preferably, the catalyst is potassium hydroxide solid or potassium hydroxide solution; the initiator is one or a mixture of more than two of glycerol, propylene glycol, diethylene glycol and sorbitol; the reaction temperature is 80-120 ℃, the reaction pressure is 0-0.4MPa, and the reaction time is 4-12 h;
preferably, the propylene oxide is used in an amount of 95 to 98 wt% of the total charge.
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| CN114225882A (en) * | 2021-12-15 | 2022-03-25 | 红宝丽集团泰兴化学有限公司 | Reaction kettle, preparation system and preparation method of polyether polyol |
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| US20220401902A1 (en) * | 2019-11-05 | 2022-12-22 | Chemical Innovation Ltd. | Polymerization installation with integrated combined absorption-diffusion and absorption-condensation unit and its application for polymer and copolymer preparation |
| CN115672230A (en) * | 2022-09-29 | 2023-02-03 | 云南云天化股份有限公司 | Alkyl phosphate oligomer preparation system and preparation method thereof |
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