CN117946380A - Preparation method and device of polyether polyol - Google Patents
Preparation method and device of polyether polyol Download PDFInfo
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- CN117946380A CN117946380A CN202211328184.5A CN202211328184A CN117946380A CN 117946380 A CN117946380 A CN 117946380A CN 202211328184 A CN202211328184 A CN 202211328184A CN 117946380 A CN117946380 A CN 117946380A
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- inner coil
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- 229920000570 polyether Polymers 0.000 title claims abstract description 58
- 239000004721 Polyphenylene oxide Substances 0.000 title claims abstract description 55
- 229920005862 polyol Polymers 0.000 title claims abstract description 42
- 150000003077 polyols Chemical class 0.000 title claims abstract description 42
- 238000002360 preparation method Methods 0.000 title abstract description 21
- 238000006243 chemical reaction Methods 0.000 claims abstract description 242
- 239000000463 material Substances 0.000 claims abstract description 131
- 125000002947 alkylene group Chemical group 0.000 claims abstract description 26
- 239000003999 initiator Substances 0.000 claims abstract description 21
- 239000002994 raw material Substances 0.000 claims abstract description 15
- 238000004519 manufacturing process Methods 0.000 claims abstract description 9
- 238000000034 method Methods 0.000 claims description 26
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims description 14
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 claims description 14
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 claims description 10
- 239000007858 starting material Substances 0.000 claims description 9
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 claims description 7
- MSXVEPNJUHWQHW-UHFFFAOYSA-N 2-methylbutan-2-ol Chemical compound CCC(C)(C)O MSXVEPNJUHWQHW-UHFFFAOYSA-N 0.000 claims description 3
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 claims description 3
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims 2
- 208000012839 conversion disease Diseases 0.000 abstract description 6
- 239000003054 catalyst Substances 0.000 description 19
- 238000002156 mixing Methods 0.000 description 13
- 238000009826 distribution Methods 0.000 description 10
- 238000005265 energy consumption Methods 0.000 description 9
- XXROGKLTLUQVRX-UHFFFAOYSA-N allyl alcohol Chemical compound OCC=C XXROGKLTLUQVRX-UHFFFAOYSA-N 0.000 description 8
- 238000012546 transfer Methods 0.000 description 8
- 230000000052 comparative effect Effects 0.000 description 7
- 238000003756 stirring Methods 0.000 description 6
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 5
- 150000001875 compounds Chemical class 0.000 description 5
- 229910052751 metal Inorganic materials 0.000 description 5
- 239000002184 metal Substances 0.000 description 5
- 238000012360 testing method Methods 0.000 description 5
- 238000011143 downstream manufacturing Methods 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 238000005259 measurement Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 235000011187 glycerol Nutrition 0.000 description 3
- 238000001308 synthesis method Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 229920005830 Polyurethane Foam Polymers 0.000 description 2
- 229910052783 alkali metal Inorganic materials 0.000 description 2
- 150000001340 alkali metals Chemical class 0.000 description 2
- 238000010923 batch production Methods 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 238000004132 cross linking Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000178 monomer Substances 0.000 description 2
- 229920002635 polyurethane Polymers 0.000 description 2
- 239000004814 polyurethane Substances 0.000 description 2
- 239000011496 polyurethane foam Substances 0.000 description 2
- 238000007151 ring opening polymerisation reaction Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 238000012644 addition polymerization Methods 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- -1 coatings Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000011437 continuous method Methods 0.000 description 1
- 239000002612 dispersion medium Substances 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 239000000806 elastomer Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
- 239000002649 leather substitute Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- NJTGANWAUPEOAX-UHFFFAOYSA-N molport-023-220-454 Chemical compound OCC(O)CO.OCC(O)CO NJTGANWAUPEOAX-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 150000002924 oxiranes Chemical class 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 229920003225 polyurethane elastomer Polymers 0.000 description 1
- 230000002028 premature Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000007142 ring opening reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- 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
-
- 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
- B01J19/0053—Details of 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
- B01J19/0066—Stirrers
-
- 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
- B01J19/1862—Stationary reactors having moving elements inside placed in series
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Polyethers (AREA)
Abstract
The invention provides a preparation method and a preparation device of polyether polyol, and relates to the technical field of polyether polyol production. The preparation method comprises the following steps: adding raw materials comprising alkylene oxide and an initiator into a first reaction kettle for reaction to obtain a material; then the materials are sent to a second reaction kettle for reaction, and the materials after the reaction in the second reaction kettle are sent to a first inner coil and a second inner coil which are connected in parallel or in series for continuous reaction, so that the polyether polyol is generated; the first inner coil is arranged in the first reaction kettle, and the second inner coil is arranged in the second reaction kettle; a preparation device of polyether polyol comprises a first reaction kettle, a second reaction kettle, a first inner coil pipe and a second inner coil pipe which are connected in series; the device utilizes two reaction kettles in series and sets up interior coil pipe in the reaction kettle, can guarantee that the material has sufficient dwell time and reaction conversion rate to reduce equipment total investment.
Description
Technical Field
The invention relates to the technical field of polyether polyol production, in particular to a preparation method and a preparation device of polyether polyol.
Background
Polyether polyol is an important intermediate for preparing polyurethane and is widely applied to the preparation of polyurethane foam plastics, elastomers, coatings, adhesives, fibers, synthetic leather, paving materials and other varieties. The maximum polyether yield is produced by using glycerin (glycerol) as an initiator and epoxide (PO and EO are commonly used together), and changing the feeding modes (mixing or separate feeding), the feeding ratio, the feeding sequence and the like of the PO and the EO. The polyether used as the polyurethane raw material can be produced by various methods. The known processes are largely divided into batch processes and continuous processes. The batch method has problems such as poor volume efficiency of the reaction tank and easy lengthening of the preparation time. The reaction tank of the continuous preparation method has high volumetric efficiency and relatively short preparation time.
The batch process mainly adopts alkali metal as a catalyst for preparing polyether polyol by ring-opening polymerization of alkylene oxide. However, propylene oxide is easily isomerized to form allyl alcohol under the action of alkali metal, and propylene oxide ring-opening polymerization is carried out on the allyl alcohol serving as an initiator to obtain monohydroxy unsaturated polyether, so that the functionality of polyether polyol is reduced, and the molecular weight distribution is widened. Such monohydroxy unsaturated polyethers can affect the properties of polyether polyols and are believed to cause premature crosslinking during the preparation of polyurethane foams, causing time-out crosslinking in the polyurethane elastomer, which alters the properties of the article.
Double metal (or multimetal) cyanide complex DMC is a catalyst for efficiently preparing polyether polyols. The DMC catalyst full-continuous polyether synthesis process is a synthesis method which adopts the continuous addition of alkylene oxide compound, initiator and catalyst to continuously lead out polyether product. The catalyst has high activity and the dosage is in the level of ppm (10 -6), so that the complex post-treatment process for removing the catalyst is not needed; the catalyst can not isomerize propylene oxide to generate allyl alcohol; meanwhile, the catalyst can also be used for preparing polyether polyol with high molecular weight and narrow molecular weight distribution. Small molecular alcohol initiators such as methanol, allyl alcohol, propylene glycol, glycerol, etc., used in conventional synthesis of polyethers, are susceptible to DMC poisoning in typical production processes, so it is generally necessary to use low molecular weight polyethers having a molecular weight of several hundred as initiators to initiate alkylene oxide polymerization.
CN113950501a discloses a process for the continuous preparation of polyoxyalkylene polyols, the present invention relates to a process for the preparation of polyoxyalkylene polyols, which comprises adding alkylene oxide to an H-functional starter substance in the presence of a Double Metal Cyanide (DMC) catalyst, wherein the alkylene oxide is metered continuously into a reactor having a reaction volume V at a mass flow rate m (alkylene oxide), the H-functional starter substance is metered continuously at a mass flow rate m (starter substance) and the Double Metal Cyanide (DMC) catalyst in a dispersion medium during the reaction at a mass flow rate m (DMC), and the resulting reaction mixture is continuously removed from the reactor, and wherein the quotient of the mass flow rate sum Σm consisting of m (alkylene oxide), m (starter substance) and m (DMC) to the reaction volume V in steady state is greater than or equal to 1200 g/(h·l).
CN103665366B discloses a method for continuously synthesizing polyether, which adopts a double-kettle double-point mode to continuously feed, the reaction kettles 1 and 2 are connected in series, and are respectively provided with a feeding point, wherein a starter, a DMC catalyst and an alkylene oxide compound are continuously added at the feeding point of the reaction kettle 1 to synthesize polyether with the designed molecular weight of 50% -99%, then the materials are continuously led out from the reaction kettle 1 to the reaction kettle 2, and the alkylene oxide compound is continuously added into the reaction kettle 2 to synthesize polyether with the designed molecular weight. The product obtained by the method not only reduces the high molecular tailing, but also obviously improves the low molecular tailing phenomenon, and has narrow molecular weight distribution.
CN103694465B discloses a continuous synthesis method of polyether, adding low molecular weight polyether into a reaction kettle, adding DMC catalyst, after nitrogen replacement, introducing alkylene oxide compound, performing induction reaction, and when the pressure is obviously reduced and the temperature is rapidly increased, indicating that the DMC catalyst has been induced; then, small molecular alcohol is adopted as a starter, alkylene oxide compounds and the starter are mixed and then are continuously added into a reaction kettle, and DMC catalysts are continuously added through an external circulation pipeline to continuously synthesize polyether products. The initiator used in the synthesis method is low in cost, the molecular weight range of the obtained polyether product is wide, the construction ratio is high, and the molecular weight distribution is narrow.
CN113429557a discloses a continuous preparation method of polyether polyol with low viscosity and narrow molecular weight distribution, which selects proper stirring power according to the concentration of catalyst in a reaction system and the difference of material residence time, and under the condition of ensuring the conversion rate of reactants, the chain transfer rate of the catalyst in the reaction process is higher than the intermolecular mixing rate, so that the safety of the device can be fully ensured, the widening of molecular weight distribution caused by overhigh mixing efficiency can be avoided, and the product achieves the effects of narrow molecular weight distribution and low viscosity.
CN1310998C discloses a continuous preparation method of polyether, which adopts a double metal cyanide complex catalyst to precisely prepare polyether with higher molecular weight. A process for continuously producing a polyether by ring-opening addition polymerization of an alkylene oxide in the presence of a double metal cyanide complex catalyst, characterized in that a gas phase part is substantially absent in a reaction apparatus, and a reaction apparatus having a multistage stirring and mixing tank is used.
The patents published at present are mostly focused on the aspects of viscosity and molecular weight distribution of polyether polyol by a continuous method, and little report is made on industrial continuous process and matched equipment, device energy consumption and reaction conversion rate.
Disclosure of Invention
In order to solve the technical problems of high energy consumption, complex flow and high equipment investment in the production and preparation process of polyether polyol in the prior art, one of the purposes of the invention is to provide a preparation method of polyether polyol, which simplifies the current process flow, realizes heat exchange between materials by utilizing the reaction heat of an inner coil pipe and the materials, can increase the heat transfer coefficient, increase the reaction conversion rate, reduce the residual monomer content and reduce the total energy consumption.
The second object of the present invention is to provide a polyether polyol production apparatus which can ensure sufficient residence time and reaction conversion rate of materials and reduce the total investment of equipment by using two reactors (reaction kettles) connected in series and an internal coil pipe provided in the reactors (reaction kettles).
In order to achieve one of the above purposes, the technical scheme adopted by the invention is as follows:
a method for preparing polyether polyol, comprising the steps of:
Adding raw materials comprising alkylene oxide and an initiator into a first reaction kettle for reaction to obtain a material; then the materials are sent to a second reaction kettle for reaction, and the materials after the reaction in the second reaction kettle are sent to a first inner coil and a second inner coil which are connected in parallel or in series for continuous reaction, so that the polyether polyol is generated;
The first inner coil is arranged in the first reaction kettle, and the second inner coil is arranged in the second reaction kettle.
In some preferred embodiments of the present invention, the alkylene oxide is at least one of ethylene oxide, propylene oxide, and butylene oxide.
In some preferred embodiments of the present invention, the initiator is a polyether polyol, and the initiator of the polyether polyol is any one of glycerol, propylene glycol, t-butanol, and t-amyl alcohol.
In some preferred embodiments of the invention, the initiator has a weight average molecular weight of 50-1000g/mol.
In some preferred embodiments of the invention, the initiator has a weight average molecular weight of 300-800g/mol.
In some preferred embodiments of the present invention, the total alkylene oxide content is 70-90wt% in weight percent; the content of the initiator is 10-30wt%. It should be noted here that the total content of alkylene oxide may be, but is not limited to, 70wt%, 72wt%, 74wt%, 76wt%, 78wt%, 80wt%, 82wt%, 84wt%, 86wt%, 88wt%, 90wt%.
In some preferred embodiments of the invention, the ratio of the circulating material of the first external circulation pump to the mass of the raw material is (15-50): 1. It should be noted that the ratio of the circulating material of the first external circulation pump to the mass of the raw material may be, but is not limited to, 15:1, 18:1, 20:1, 22:1, 25:1, 28:1, 30:1, 32:1, 35:1, 38:1, 40:1, 42:1, 45:1, 48:1, 50:1.
In some preferred embodiments of the invention, the ratio of the circulating material of the first external circulation pump to the mass of the raw material is (20-40): 1.
In some preferred embodiments of the present invention, the ratio of the circulating material of the second external circulation pump to the mass of the material flowing into the second reaction vessel is (15-50): 1. It should be noted that the ratio of the circulating material of the first external circulation pump to the mass of the raw material may be, but is not limited to, 15:1, 18:1, 20:1, 22:1, 25:1, 28:1, 30:1, 32:1, 35:1, 38:1, 40:1, 42:1, 45:1, 48:1, 50:1.
In some preferred embodiments of the invention, the ratio of the mass of the circulating material of the second external circulation pump to the mass of the material flowing into the second reaction vessel is (20-40): 1.
In some preferred embodiments of the present invention, the material in the first reaction kettle is cooled by the first circulating heat exchanger and then returned to the first reaction kettle.
In some preferred embodiments of the present invention, the material in the second reaction vessel is cooled by the second circulating heat exchanger and then returned to the second reaction vessel.
In some preferred embodiments of the invention, the ratio of the pump circulation to the mass of the feedstock is (20-40): 1.
In some preferred embodiments of the invention, the ratio of the pump circulation to the mass of the feedstock is (20-40): 1.
In some preferred embodiments of the invention, the pressure of the first reaction vessel is 0.2-0.5MPaG. Here, the pressure of the first reaction vessel may be, but not limited to, 0.2MPaG, 0.3MPaG, 0.4MPaG, 0.5MPaG.
In some preferred embodiments of the invention, the pressure of the first reaction vessel is 0.3-0.4MPaG.
In some preferred embodiments of the invention, the pressure of the second reaction vessel is 0.2-0.5MPaG. Here, the pressure of the second reaction vessel may be, but not limited to, 0.2MPaG, 0.3MPaG, 0.4MPaG, 0.5MPaG.
In some preferred embodiments of the invention, the pressure of the second reactor is 0.28-0.38MPaG.
In some preferred embodiments of the present invention, when the first inner coil and the second inner coil are connected in series, the material in the second reaction vessel is sent to the first inner coil, flows out of the first inner coil, then is sent to the second inner coil, and then flows out of the second inner coil.
In some preferred embodiments of the present invention, when the first inner coil and the second inner coil are connected in series, the material in the second reaction vessel is sent to the second inner coil, flows out of the second inner coil, then is sent to the first inner coil, and then flows out of the first inner coil.
In some preferred embodiments of the present invention, when the first inner coil and the second inner coil are connected in parallel, the material in the second reaction kettle is split into two streams and sent to the first inner coil and the second inner coil respectively, and the material flowing out of the first inner coil and the material flowing out of the second inner coil are converged and then flow out together.
In order to achieve the second purpose, the technical scheme adopted by the invention is as follows:
A polyether polyol production apparatus for carrying out the above-described method, comprising:
the first reaction kettle and the second reaction kettle are connected in series;
The first inner coil is arranged in the first reaction kettle;
the second inner coil is arranged in the second reaction kettle;
The first inner coil pipe and the second inner coil pipe are connected with a discharge hole of the second reaction kettle in a serial connection mode or a parallel connection mode.
In some preferred embodiments of the present invention, a first feeding port is formed at the bottom of the first reaction kettle, and a first discharging port is formed at the top of the first reaction kettle.
In some preferred embodiments of the present invention, a second feeding port is formed at the bottom of the second reaction kettle, and a second discharging port is formed at the top of the second reaction kettle.
In some preferred embodiments of the present invention, when the first inner coil and the second inner coil are connected in series, the second outlet is connected to the inlet of the first inner coil, and the outlet of the first inner coil is connected to the inlet of the second inner coil.
In some preferred embodiments of the present invention, when the first inner coil and the second inner coil are connected in series, the second outlet is connected to the inlet of the second inner coil, and the outlet of the second inner coil is connected to the inlet of the first inner coil.
In some preferred embodiments of the present invention, when the first inner coil and the second inner coil are connected in parallel, the second outlet is connected to the inlet of the first inner coil and the inlet of the second inner coil, respectively.
In some preferred embodiments of the present invention, the feed inlet of the first inner coil is located at the bottom of the first reaction vessel, and the discharge outlet of the first inner coil is located at the top side wall of the first reaction vessel.
In some preferred embodiments of the present invention, the feed inlet of the second inner coil is located at the bottom of the second reactor, and the discharge outlet of the second inner coil is located at the top side wall of the second reactor.
In some preferred embodiments of the invention, the first inner coil and/or the second inner coil is in a spiral configuration.
In some preferred embodiments of the present invention, a first circulation outlet arranged at the bottom of the first reaction kettle is connected with a material inlet of a first external circulation heat exchanger, a material outlet of the first external circulation heat exchanger is connected with a first circulation inlet arranged at the top of the first reaction kettle, and a first external circulation pump is arranged on a pipeline connecting the first circulation outlet and the material inlet of the first external circulation heat exchanger.
In some preferred embodiments of the present invention, a second circulation outlet arranged at the bottom of the second reaction kettle is connected with a material inlet of a second external circulation heat exchanger, the material outlet of the second external circulation heat exchanger is connected with a second circulation inlet arranged at the top of the second reaction kettle, and a second external circulation pump is arranged on a pipeline connecting the second circulation outlet and the material inlet of the second external circulation heat exchanger.
In some preferred embodiments of the invention, the temperature of the first external circulation heat exchanger material outlet is 120-150 ℃.
In some preferred embodiments of the invention, the temperature of the first external circulation heat exchanger material outlet is 130-140 ℃.
In some preferred embodiments of the invention, the temperature of the second external circulation heat exchanger material outlet is 120-150 ℃.
In some preferred embodiments of the invention, the temperature of the second external circulation heat exchanger material outlet is 130-140 ℃.
It should be noted that the temperatures of the first external circulation heat exchanger material outlet and the second external circulation heat exchanger material outlet may be, but are not limited to, 120 ℃, 125 ℃, 130 ℃, 135 ℃, 140 ℃, 145 ℃, 150 ℃.
In some preferred embodiments of the invention, the first inner coil has a diameter of 25-300mm.
In some preferred embodiments of the invention, the first inner coil has a diameter of 40-200mm.
In some preferred embodiments of the invention, the second inner coil has a diameter of 25-300mm.
In some preferred embodiments of the invention, the second inner coil has a diameter of 40-200mm.
The diameters of the first inner coil and the second inner coil may be, but are not limited to, 25mm, 40mm, 50mm, 65mm, 80mm, 100mm, 125mm, 150mm, 200mm, 250mm, 300mm.
In some preferred embodiments of the invention, the ratio of the pitch to the diameter of the first inner coil is (1-5): 1.
In some preferred embodiments of the invention, the ratio of the pitch to the diameter of the first inner coil is (1.25-2): 1.
In some preferred embodiments of the invention, the ratio of the pitch to the diameter of the second inner coil is (1-5): 1.
In some preferred embodiments of the invention, the ratio of the pitch to the diameter of the second inner coil is (1.25-2): 1.
It should be noted that the ratio of the pitch to the diameter of the first inner coil and the second inner coil may be, but is not limited to, 1:1, 2:1, 3:1, 4:1, 5:1.
In some preferred embodiments of the invention, the ratio of the wheel diameter of the first inner coil to the diameter of the first reactor is (0.4-0.95): 1.
In some preferred embodiments of the invention, the ratio of the wheel diameter of the first inner coil to the diameter of the first reactor is (0.5-0.85): 1.
In some preferred embodiments of the invention, the ratio of the diameter of the second inner coil to the diameter of the second reactor is (0.4-0.95): 1.
In some preferred embodiments of the invention, the ratio of the diameter of the second inner coil to the diameter of the second reactor is (0.5-0.85): 1.
It should be noted that, the ratio of the wheel diameter of the first inner coil to the wheel diameter of the second inner coil to the diameter of the reaction kettle may be, but not limited to, 0.4:1, 0.5:1, 0.6:1, 0.7:1, 0.8:1, 0.9:1, 0.95:1.
In some preferred embodiments of the present invention, a jacket and/or a stirrer are further provided in the first reaction vessel and/or the second reaction vessel.
Compared with the prior art, the embodiment of the application has at least the following advantages or beneficial effects:
1. According to the preparation method of polyether polyol, heat exchange between materials is realized by utilizing the reaction heat of the inner coil pipe and the materials, so that the heat transfer coefficient can be increased, the reaction conversion rate can be increased, the residual monomer content can be reduced, and the total energy consumption can be reduced.
2. The device provided by the invention utilizes two reactors (reaction kettles) connected in series and an inner coil pipe arranged in the reactors (reaction kettles), so that the material can be ensured to have enough residence time and reaction conversion rate, and the total equipment investment is reduced.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings that are needed in the embodiments will be briefly described below, it being understood that the following drawings only illustrate some embodiments of the present application and therefore should not be considered as limiting the scope, and other related drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic structural diagram of embodiment 1 of the present invention;
FIG. 2 is a schematic structural diagram of embodiment 9 of the present invention;
FIG. 3 is a schematic diagram of an embodiment 10 of the present invention;
Fig. 4 is a schematic structural view of comparative example 1 of the present invention.
Icon: 100-a first reaction kettle, 101-a first feed inlet, 102-a first discharge outlet, 103-a first inner coil, 1031-a first inner coil feed inlet, 1032-a first inner coil discharge outlet, 104-a first outer circulation pump, 1041-a first circulation pump feed inlet, 105-a first outer circulation heat exchanger, 200-a second reaction kettle, 201-a second discharge outlet, 202-a second inner coil, 2021-a second inner coil feed inlet, 2022-a second inner coil discharge outlet, 203-a second outer circulation pump, 2031-a second circulation pump feed inlet, 204-a second outer circulation heat exchanger, 205-a second feed inlet, 300-a third reaction kettle, 301-a third discharge outlet, 302-a third outer circulation pump, 3021-a third circulation pump feed inlet, 303-a third outer circulation heat exchanger.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention more clear, the technical solutions of the embodiments of the present invention will be clearly and completely described below. The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or apparatus used were conventional products commercially available without the manufacturer's attention.
It should be noted that, without conflict, the embodiments of the present invention and features in the embodiments may be combined with each other, and the present invention will be described in detail with reference to specific embodiments.
The working principle of fig. 1 is: introducing reaction raw materials containing alkylene oxide and an initiator into a first reaction kettle 100 from a first feed inlet 101 at the bottom of the first reaction kettle 100, stirring and uniformly mixing, and fully reacting and transferring heat; the reacted materials flow out from a first discharge hole 102 at the top of the first reaction kettle 100 and then enter a second reaction kettle 200 from a second feed hole 205 at the bottom of the second reaction kettle 200, and the materials are continuously stirred and uniformly mixed, reacted and subjected to heat transfer in the second reaction kettle 200; the reacted material flows out from a second discharge port 201 at the top of the second reaction kettle 200. The material flow flowing out from the top of the second reaction kettle 200 is divided into two parts, the first material flow is sent into the second inner coil 202 from the second inner coil feed inlet 2021, flows out from the second inner coil discharge outlet 2022 after fully exchanging heat and reacting with the material in the second reaction kettle 200, and the second material flow is sent into the first inner coil 103 from the first inner coil feed inlet 1031, flows out from the first inner coil discharge outlet 1032 after fully exchanging heat and reacting with the material in the first reaction kettle 100; and after the second inner coil effluent flow and the first inner coil effluent flow are combined, the combined second inner coil effluent flow and the combined first inner coil effluent flow are sent to a downstream process for post-treatment refining to obtain a polyether polyol product, wherein the post-treatment comprises the steps of further removing sheets, heat exchange, filtering, storing and the like.
The effluent flow at the bottom of the first reaction kettle 100 enters the first external circulation pump 104 through the first circulation pump feed inlet 1041, and is cooled by the first external circulation heat exchanger 105, and the cooled effluent flow is circulated to the first reaction kettle 100. The material flow discharged from the bottom of the kettle is the same as the material flow discharged from the top of the kettle, and the external circulating pump is used for controlling the full mixing of materials in the kettle on one hand and timely removing the heat released by the reaction in the kettle on the other hand.
The material flow at the bottom of the second reaction kettle 200 flows into the second external circulation pump 203 through the second circulation pump feed port 2031, and is cooled by the second external circulation heat exchanger 204, the cooled material flow is circulated to the second reaction kettle 200, the mixing of materials in the reaction kettles is enhanced (the first reaction kettle and the second reaction kettle are respectively provided with a stirrer, and the rotating speed of the stirrer is controlled to be 100-150 rpm/min), and the temperature of the materials in the reaction kettles is controlled.
The working principle of fig. 2 is: introducing reaction raw materials containing alkylene oxide and an initiator into a first reaction kettle 100 from a first feed inlet 101 at the bottom of the first reaction kettle 100, stirring and uniformly mixing, and fully reacting and transferring heat; the reacted materials flow out from a first discharge hole 102 at the top of the first reaction kettle 100 and then enter a second reaction kettle 200 from a second feed hole 205 at the bottom of the second reaction kettle 200, and the materials are continuously stirred and uniformly mixed, reacted and subjected to heat transfer in the second reaction kettle 200; the reacted material flows out from a second discharge port 201 at the top of the second reaction kettle 200. The material flow flowing out from the top of the second reaction kettle 200 is sent to the first inner coil 103, and flows out from the discharge hole 1032 of the first inner coil after fully exchanging heat and reacting with the material in the first reaction kettle 100; the material at the outlet of the first inner coil pipe is sent to the second inner coil pipe 202, and flows out of the second inner coil pipe 202 after fully exchanging heat and reacting with the material in the second reaction kettle 200; the effluent stream of the second inner coil is sent to a downstream process for post-treatment to obtain a polyether polyol product, wherein the post-treatment comprises the steps of further removing sheets, exchanging heat, filtering, storing and the like.
The effluent flow at the bottom of the first reaction kettle 100 enters the first external circulation pump 104 through the first circulation pump feed inlet 1041, and is cooled by the first external circulation heat exchanger 105, and the cooled effluent flow is circulated to the first reaction kettle 100.
The material flow at the bottom of the second reaction kettle 200 flows into the second external circulation pump 203 through the second circulation pump feed port 2031, and is cooled by the second external circulation heat exchanger 204, the cooled material flow is circulated to the second reaction kettle 200, the mixing of materials in the reaction kettles is enhanced (the first reaction kettle and the second reaction kettle are respectively provided with a stirrer, and the rotating speed of the stirrer is controlled to be 100-150 rpm/min), and the temperature of the materials in the reaction kettles is controlled.
The working principle of fig. 3 is: introducing reaction raw materials containing alkylene oxide and an initiator into a first reaction kettle 100 from a first feed inlet 101 at the bottom of the first reaction kettle 100, stirring and uniformly mixing, and fully reacting and transferring heat; the reacted materials flow out from a first discharge hole 102 at the top of the first reaction kettle 100 and then enter a second reaction kettle 200 from a second feed hole 205 at the bottom of the second reaction kettle 200, and the materials are continuously stirred and uniformly mixed, reacted and subjected to heat transfer in the second reaction kettle 200; the reacted material flows out from a second discharge port 201 at the top of the second reaction kettle 200. The material flow flowing out from the top of the second reaction kettle 200 is sent to the second inner coil 202 from the second inner coil feed inlet 2021, and flows out from the second inner coil discharge outlet 2022 after fully exchanging heat and reacting with the material in the second reaction kettle 200; delivering the second inner coil outlet material from the first inner coil feed inlet 1031 to the first inner coil 103, and flowing out from the first inner coil discharge outlet 1032 after fully exchanging heat and reacting with the material in the first reaction kettle 100; the effluent stream of the second inner coil is sent to a downstream process for post-treatment to obtain a polyether polyol product, wherein the post-treatment comprises the steps of further removing sheets, exchanging heat, filtering, storing and the like.
The effluent flow at the bottom of the first reaction kettle 100 enters the first external circulation pump 104 through the first circulation pump feed inlet 1041, and is cooled by the first external circulation heat exchanger 105, and the cooled effluent flow is circulated to the first reaction kettle 100.
The material flow at the bottom of the second reaction kettle 200 flows into the second external circulation pump 203 through the second circulation pump feed port 2031, and is cooled by the second external circulation heat exchanger 204, the cooled material flow is circulated to the second reaction kettle 200, the mixing of materials in the reaction kettles is enhanced (the first reaction kettle and the second reaction kettle are respectively provided with a stirrer, and the rotating speed of the stirrer is controlled to be 100-150 rpm/min), and the temperature of the materials in the reaction kettles is controlled.
The working principle of fig. 4 is: introducing reaction raw materials containing alkylene oxide and an initiator into a first reaction kettle 100 from a first feed inlet 101 at the bottom of the first reaction kettle 100, stirring and uniformly mixing, and fully reacting and transferring heat; the reacted materials flow out from a first discharge hole 102 at the top of the first reaction kettle 100 and then enter a second reaction kettle 200 from a second feed hole 205 at the bottom of the second reaction kettle 200, and the materials are continuously stirred and uniformly mixed, reacted and subjected to heat transfer in the second reaction kettle 200; the reacted materials flow out from the second discharge port 201 at the top of the second reaction kettle 200, then enter the third reaction kettle 300 from the third feed port at the bottom of the third reaction kettle 300, and are continuously stirred and mixed uniformly in the third reaction kettle 300, reacted and subjected to heat transfer, and then flow out from the third discharge port 301 at the top of the third reaction kettle 300. And delivering the flow flowing out from the top of the third reaction kettle 300 to a downstream process for post-treatment to obtain a polyether polyol product, wherein the post-treatment comprises the steps of further removing sheets, exchanging heat, filtering, storing and the like.
The effluent flow at the bottom of the first reaction kettle 100 enters the first external circulation pump 104 through the first circulation pump feed inlet 1041, and is cooled by the first external circulation heat exchanger 105, and the cooled effluent flow is circulated to the first reaction kettle 100.
The material flow at the bottom of the second reaction kettle 200 flows into the second external circulation pump 203 through the second circulation pump feed port 2031, is cooled by the second external circulation heat exchanger 204, and circulates to the second reaction kettle 200 to strengthen the mixing of materials in the reaction kettle and control the temperature of the materials in the kettle.
The effluent flow at the bottom of the third reaction kettle 300 flows into the third external circulation pump 302 through the third circulation pump feed inlet 3021, and is cooled by the third external circulation heat exchanger 303, and the cooled effluent flow is circulated to the third reaction kettle 300. The first, second and third reaction kettles are respectively provided with a stirrer, and the rotating speed of the stirrers is controlled to be 100-150rpm/min.
Example 1
Referring to FIG. 1, the feed stream flow rate 9376kg/h, in weight percent, comprises: 70% by weight of propylene oxide, 13% by weight of ethylene oxide, 17% by weight of polyether polyol containing glycerol structures and having a molecular weight of 500 g/mol.
The operating pressure of the first reaction kettle is 0.3MPaG, the temperature in the first reaction kettle is 140 ℃, the temperature of the material outlet of the first external circulation heat exchanger is 130 ℃, the circulation ratio of the first external circulation heat exchanger is 20:1 (namely the mass ratio of the circulating material of the first external circulation pump to the reaction raw material), the diameter of the first internal coil pipe is 50mm, the ratio of the coil pipe pitch to the coil pipe diameter is 1.5:1, the ratio of the coil pipe diameter to the reaction kettle diameter is 0.65:1, and the rotating speed is 120rpm.
The operating pressure of the second reaction kettle is 0.28MPaG, the temperature in the second reaction kettle is 140 ℃, the temperature at the material outlet of the second external circulation heat exchanger is 130 ℃, the circulation ratio of the second external circulation heat exchanger (namely, the mass ratio of the circulating material of the second external circulation pump to the material flowing into the second reaction kettle) is 20:1, the diameter of the second internal coil pipe is 50mm, the ratio of the coil pipe pitch to the coil pipe diameter is 1.5:1, the ratio of the coil pipe diameter to the reaction kettle diameter is 0.65:1, and the rotating speed is 120rpm.
Example 2
This embodiment is substantially the same as embodiment 1 except that: the temperature of the material outlet of the first external circulation heat exchanger and the material outlet of the second external circulation heat exchanger are 132 ℃.
Example 3
This embodiment is substantially the same as embodiment 1 except that: the temperature of the material outlet of the first external circulation heat exchanger and the material outlet of the second external circulation heat exchanger are 134 ℃.
Example 4
This embodiment is substantially the same as embodiment 1 except that: the temperature in the first reaction kettle and the temperature in the second reaction kettle are 142 ℃.
Example 5
This embodiment is substantially the same as embodiment 4 except that: the temperature of the material outlet of the first external circulation heat exchanger and the material outlet of the second external circulation heat exchanger are 132 ℃.
Example 6
This embodiment is substantially the same as embodiment 1 except that: the temperature in the first reaction kettle and the temperature in the second reaction kettle are 138 ℃.
Example 7
This embodiment is substantially the same as embodiment 1 except that: the circulation ratio of the first external circulation heat exchanger and the circulation ratio of the second external circulation heat exchanger are both 30:1.
Example 8
This embodiment is substantially the same as embodiment 1 except that: 1. the diameter of the first inner coil pipe and the diameter of the second inner coil pipe are both 150mm, the ratio of the coil pipe pitch to the coil pipe diameter is 1.25:1, and the ratio of the coil pipe diameter to the diameter of the reaction kettle is 0.85:1; 2. the circulation ratio of the first external circulation heat exchanger and the circulation ratio of the second external circulation heat exchanger are both 30:1.
Example 9
This embodiment is substantially the same as embodiment 3 except that: the process flow is shown in fig. 2.
Example 10
This embodiment is substantially the same as embodiment 3 except that: the process flow is shown in fig. 3.
Example 11
The feed stream comprises, in weight percent: 70wt% propylene oxide, 13wt% ethylene oxide, 17wt% molecular weight 800 polyether polyol (starter+catalyst) containing glycerol and propylene glycol structures, the process flow being shown in FIG. 1.
The operation pressure of the first reaction kettle is 0.2MPaG, the temperature in the first reaction kettle is 120 ℃, the temperature of a material outlet of the first external circulation heat exchanger is 110 ℃, the circulation ratio of the first external circulation heat exchanger is 15:1, the diameter of the first internal coil pipe is 50mm, the ratio of the coil pipe pitch to the coil pipe diameter is 1.25:1, the ratio of the coil pipe diameter to the reaction kettle diameter is 0.65:1, and the rotating speed is 120rpm.
The operating pressure of the second reaction kettle is 0.2MPaG, the temperature in the second reaction kettle is 120 ℃, the material outlet temperature of the second external circulation heat exchanger is 110 ℃, the circulation ratio of the second external circulation heat exchanger is 15:1, the diameter of the second internal coil pipe is 50mm, the ratio of the coil pipe pitch to the coil pipe diameter is 1.25:1, the ratio of the coil pipe diameter to the reaction kettle diameter is 0.65:1, and the rotating speed is 120rpm.
Example 12
Referring to fig. 1, the feed stream comprises, in weight percent: 70wt% propylene oxide, 12wt% ethylene oxide, 1.0wt% butylene oxide, 17wt% polyether polyol having a molecular weight of 500g/mol and a glycerol structure.
The operation pressure of the first reaction kettle is 0.3MPaG, the temperature in the first reaction kettle is 140 ℃, the temperature of the material outlet of the first external circulation heat exchanger is 134 ℃, the circulation ratio of the first external circulation heat exchanger is 20:1, the diameter of the first internal coil pipe is 50mm, the ratio of the coil pipe pitch to the coil pipe diameter is 1.5:1, the ratio of the coil pipe diameter to the reaction kettle diameter is 0.65:1, and the rotating speed is 120rpm.
The operating pressure of the second reaction kettle is 0.28MPaG, the temperature in the second reaction kettle is 140 ℃, the material outlet temperature of the second external circulation heat exchanger is 134 ℃, the circulation ratio of the second external circulation heat exchanger is 20:1, the diameter of the second internal coil pipe is 50mm, the ratio of the coil pipe pitch to the coil pipe diameter is 1.5:1, the ratio of the coil pipe diameter to the reaction kettle diameter is 0.65:1, and the rotating speed is 120rpm.
Example 13
Referring to fig. 1, the feed stream comprises, in weight percent: 70wt% of propylene oxide, 13wt% of ethylene oxide, 17wt% of a polyether polyol having a propylene glycol and a propylene glycol structure and a molecular weight of 500.
The operation pressure of the first reaction kettle is 0.5MPaG, the temperature in the first reaction kettle is 145 ℃, the temperature of the material outlet of the first external circulation heat exchanger is 135 ℃, the circulation ratio of the first external circulation heat exchanger is 50:1, the diameter of the first internal coil pipe is 50mm, the ratio of the coil pipe pitch to the coil pipe diameter is 2.5:1, the ratio of the coil pipe diameter to the reaction kettle diameter is 0.95:1, and the rotating speed is 120rpm.
The operating pressure of the second reaction kettle is 0.5MPaG, the temperature in the second reaction kettle is 145 ℃, the material outlet temperature of the second external circulation heat exchanger is 135 ℃, the circulation ratio of the second external circulation heat exchanger is 50:1, the diameter of the second internal coil pipe is 50mm, the ratio of the coil pipe pitch to the coil pipe diameter is 2.5:1, the ratio of the coil pipe diameter to the reaction kettle diameter is 0.95:1, and the rotating speed is 120rpm.
Comparative example 1
Referring to fig. 4, the feed stream comprises, in weight percent: 70wt% propylene oxide, 13wt% ethylene oxide, 17wt% low molecular weight polyether polyol.
The operating pressure of the first reaction kettle is 0.3MPaG, the temperature in the first reaction kettle is 140 ℃, the temperature of the material outlet of the first external circulation heat exchanger is 130 ℃, and the circulation ratio of the first external circulation heat exchanger is 20.
The operating pressure of the second reaction kettle is 0.28MPaG, the temperature in the second reaction kettle is 140 ℃, the temperature of the material outlet of the second external circulation heat exchanger is 130 ℃, and the circulation ratio of the second external circulation heat exchanger is 20:1.
The operating pressure of the third reaction kettle is 0.26MPaG, the temperature in the third reaction kettle is 140 ℃, the temperature of a discharge hole of the third external circulation heat exchanger is 130 ℃, and the circulation ratio of the third external circulation heat exchanger is 20:1.
Comparative example 2
This comparative example is substantially the same as comparative example 1, except that: the temperature in the first reaction kettle, the second reaction kettle and the third reaction kettle is 142 ℃.
Test examples
In this test example, the products produced in comparative examples 1 and 2 were subjected to an alkylene oxide total conversion measurement test, an energy consumption measurement test, and a molecular weight distribution index measurement test, respectively, for examples 1 to 13; wherein the energy consumption calculation was performed with reference to national standard GB/T50441-2016, the molecular weight and the molecular weight distribution index were measured according to GPC, and the measurement results are shown in Table 1.
TABLE 1
The production processes and apparatuses adopted in comparative examples 1 and 2 are all the processes and apparatuses commonly used at present, and as can be seen from the data in table 1, the preparation method and apparatus for polyether polyol provided by the invention can not only achieve the total conversion rate of alkylene oxide in the conventional processes, but also reduce the energy consumption and the total investment of equipment to a certain extent. The greater energy consumption of example 13 is due to the higher reaction temperature and greater circulation, thus significantly increasing utility and pump motor energy consumption.
It should be noted that the above-described embodiments are only for explaining the present invention and do not constitute any limitation of the present invention. The invention has been described with reference to exemplary embodiments, but it is understood that the words which have been used are words of description and illustration, rather than words of limitation. Modifications may be made to the invention as defined in the appended claims, and the invention may be modified without departing from the scope and spirit of the invention. Although the invention is described herein with reference to particular means, materials and embodiments, the invention is not intended to be limited to the particulars disclosed herein, as the invention extends to all other means and applications which perform the same function.
Claims (12)
1. A process for preparing a polyether polyol comprising the steps of:
Adding raw materials comprising alkylene oxide and an initiator into a first reaction kettle for reaction to obtain a material; then the materials are sent to a second reaction kettle for reaction, and the materials after the reaction in the second reaction kettle are sent to a first inner coil and a second inner coil which are connected in parallel or in series for continuous reaction, so that the polyether polyol is generated;
The first inner coil is arranged in the first reaction kettle, and the second inner coil is arranged in the second reaction kettle.
2. The method of claim 1, wherein the alkylene oxide is at least one of ethylene oxide, propylene oxide, and butylene oxide;
And/or the initiator is polyether polyol, and the initiator of the polyether polyol is any one of glycerol, propylene glycol, tertiary butanol and tertiary amyl alcohol; preferably, the starter has a weight average molecular weight of 50-1000g/mol, preferably 300-800g/mol;
and/or, the content of the alkylene oxide in the raw material is 70-90wt% in percentage by weight; the content of the initiator is 10-30wt%.
3. The method according to claim 1 or 2, wherein the materials in the first reaction kettle flow into the first circulating heat exchanger through the first external circulating pump for cooling, the cooled materials are returned into the first reaction kettle, and/or the materials in the second reaction kettle flow into the second circulating heat exchanger through the second external circulating pump for cooling, and the cooled materials are returned into the second reaction kettle;
Preferably, the method comprises the steps of,
The temperature of the material outlet of the first external circulation heat exchanger is 120-150 ℃, preferably 130-140 ℃;
and/or the temperature of the material outlet of the second external circulation heat exchanger is 120-150 ℃, preferably 130-140 ℃.
4. A method according to claim 3, characterized in that the ratio of the mass of the circulating material of the first external circulation pump to the mass of the raw material is (15-50): 1, preferably (20-40): 1;
And/or the ratio of the circulating material of the second external circulation pump to the material flowing into the second reaction kettle is (15-50): 1, preferably (20-40): 1.
5. The process according to any one of claims 1 to 4, wherein the first reactor is operated at a pressure of 0.2 to 0.5MPaG, preferably 0.3 to 0.4MPaG;
And/or the operating pressure of the second reaction kettle is 0.2-0.5MPaG, preferably 0.28-0.38MPaG.
6. The method according to any one of claims 1 to 5, wherein when the first inner coil and the second inner coil are connected in series, the material in the second reaction kettle is sent to the first inner coil, flows out of the first inner coil and then is sent to the second inner coil, and then flows out of the second inner coil, and/or the material in the second reaction kettle is sent to the second inner coil, flows out of the second inner coil and then is sent to the first inner coil, and then flows out of the first inner coil;
And/or when the first inner coil and the second inner coil are connected in parallel, the materials in the second reaction kettle are divided into two strands and respectively sent to the first inner coil and the second inner coil, and the materials flowing out of the first inner coil and the materials flowing out of the second inner coil are converged and then flow out together.
7. A production apparatus for polyether polyol, for carrying out the method according to any one of claims 1 to 6, comprising:
the first reaction kettle and the second reaction kettle are connected in series;
The first inner coil is arranged in the first reaction kettle;
the second inner coil is arranged in the second reaction kettle;
The first inner coil pipe and the second inner coil pipe are connected with a discharge hole of the second reaction kettle in a serial connection mode or a parallel connection mode.
8. The device of claim 7, wherein a first feed port is formed in the bottom of the first reaction kettle, and a first discharge port is formed in the top of the first reaction kettle;
And/or, a second feeding port is formed in the bottom of the second reaction kettle, and a second discharging port is formed in the top of the second reaction kettle.
9. The apparatus of claim 8, wherein when the first inner coil and the second inner coil are connected in series, the second outlet is connected to the inlet of the first inner coil, the outlet of the first inner coil is connected to the inlet of the second inner coil, and/or the second outlet is connected to the inlet of the second inner coil, the outlet of the second inner coil is connected to the inlet of the first inner coil;
And/or when the first inner coil pipe and the second inner coil pipe are connected in parallel, the second discharge port is respectively connected with the feed inlet of the first inner coil pipe and the feed inlet of the second inner coil pipe;
and/or the feed inlet of the first inner coil is positioned at the bottom of the first reaction kettle, and the discharge outlet of the first inner coil is positioned at the side wall of the top of the first reaction kettle;
and/or the feed inlet of the second inner coil is positioned at the bottom of the second reaction kettle, and the discharge outlet of the second inner coil is positioned at the side wall of the top of the second reaction kettle;
and/or the first inner coil and/or the second inner coil are in a spiral structure.
10. The device according to any one of claims 7 to 9, wherein a first circulation outlet arranged at the bottom of the first reaction kettle is connected with a material inlet of a first external circulation heat exchanger, the material outlet of the first external circulation heat exchanger is connected with a first circulation inlet arranged at the top of the first reaction kettle, and a first external circulation pump is arranged on a pipeline connecting the first circulation outlet and the material inlet of the first external circulation heat exchanger;
And/or a second circulating outlet arranged at the bottom of the second reaction kettle is connected with a material inlet of a second external circulating heat exchanger, the material outlet of the second external circulating heat exchanger is connected with a second circulating inlet arranged at the top of the second reaction kettle, and a second external circulating pump is arranged on a pipeline connecting the second circulating outlet with the material inlet of the second external circulating heat exchanger;
Preferably, the method comprises the steps of,
The temperature of the material outlet of the first external circulation heat exchanger is 120-150 ℃, preferably 130-140 ℃;
and/or the temperature of the material outlet of the second external circulation heat exchanger is 120-150 ℃, preferably 130-140 ℃.
11. The device according to any one of claims 7-10, wherein the first and second inner coils are the same or different in diameter, each independently being 25-300mm, preferably 40-200mm;
and/or the ratio of the pitch to the diameter of the first and second inner coils is the same or different and is each independently (1-5): 1, preferably (1.25-2): 1;
And/or the ratio of the diameter of the first inner coil to the diameter of the first reaction kettle and the ratio of the diameter of the second inner coil to the diameter of the second reaction kettle are the same or different, and are each independently (0.4-0.95): 1, preferably (0.5-0.85): 1.
12. The apparatus according to any one of claims 7 to 11, wherein a jacket and/or a stirrer is further provided in the first reaction vessel and/or the second reaction vessel.
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