CN111978273A - Continuous synthesis process of epoxy chloropropane by hydrogen peroxide method - Google Patents
Continuous synthesis process of epoxy chloropropane by hydrogen peroxide method Download PDFInfo
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- CN111978273A CN111978273A CN202010992565.8A CN202010992565A CN111978273A CN 111978273 A CN111978273 A CN 111978273A CN 202010992565 A CN202010992565 A CN 202010992565A CN 111978273 A CN111978273 A CN 111978273A
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- hydrogen peroxide
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- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 title claims abstract description 97
- 238000000034 method Methods 0.000 title claims abstract description 47
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 19
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 19
- LRWZZZWJMFNZIK-UHFFFAOYSA-N 2-chloro-3-methyloxirane Chemical compound CC1OC1Cl LRWZZZWJMFNZIK-UHFFFAOYSA-N 0.000 title claims abstract description 9
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 111
- 239000003054 catalyst Substances 0.000 claims abstract description 45
- OWXJKYNZGFSVRC-NSCUHMNNSA-N (e)-1-chloroprop-1-ene Chemical compound C\C=C\Cl OWXJKYNZGFSVRC-NSCUHMNNSA-N 0.000 claims abstract description 27
- BRLQWZUYTZBJKN-UHFFFAOYSA-N Epichlorohydrin Chemical compound ClCC1CO1 BRLQWZUYTZBJKN-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000006243 chemical reaction Methods 0.000 claims abstract description 21
- 238000002156 mixing Methods 0.000 claims abstract description 10
- VLEVUVPHNDEWGB-UHFFFAOYSA-N 1-chloroprop-1-ene methanol Chemical compound CO.ClC=CC VLEVUVPHNDEWGB-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000011259 mixed solution Substances 0.000 claims abstract description 5
- 238000006735 epoxidation reaction Methods 0.000 claims abstract description 4
- 230000002194 synthesizing effect Effects 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 2
- 239000012295 chemical reaction liquid Substances 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 claims description 2
- 239000000376 reactant Substances 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 37
- 239000008367 deionised water Substances 0.000 description 21
- 229910021641 deionized water Inorganic materials 0.000 description 21
- 239000000463 material Substances 0.000 description 13
- 238000007599 discharging Methods 0.000 description 12
- 238000011049 filling Methods 0.000 description 9
- 230000014759 maintenance of location Effects 0.000 description 6
- 238000005086 pumping Methods 0.000 description 6
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- UGACIEPFGXRWCH-UHFFFAOYSA-N [Si].[Ti] Chemical compound [Si].[Ti] UGACIEPFGXRWCH-UHFFFAOYSA-N 0.000 description 2
- 239000013064 chemical raw material Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000007036 catalytic synthesis reaction Methods 0.000 description 1
- 125000001309 chloro group Chemical group Cl* 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- -1 coatings Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 125000003700 epoxy group Chemical group 0.000 description 1
- 239000003822 epoxy resin Substances 0.000 description 1
- 239000011152 fibreglass Substances 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 150000002924 oxiranes Chemical class 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 229920000647 polyepoxide Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000005060 rubber Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 239000008247 solid mixture Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/02—Synthesis of the oxirane ring
- C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
- C07D301/12—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D303/00—Compounds containing three-membered rings having one oxygen atom as the only ring hetero atom
- C07D303/02—Compounds containing oxirane rings
- C07D303/08—Compounds containing oxirane rings with hydrocarbon radicals, substituted by halogen atoms, nitro radicals or nitroso radicals
Abstract
The invention provides a continuous synthesis process of epoxy chloropropane by a hydrogen peroxide method, which comprises the steps of putting hydrogen peroxide, methanol, chloropropene and a catalyst into a reactor for epoxidation, wherein the reactor is a ring reactor, the catalyst is pre-loaded into the ring reactor, chloropropene and methanol form a chloropropene-methanol mixed solution in a mixing tank, and the chloropropene-methanol mixed solution is pumped into the ring reactor by a metering pump A, and hydrogen peroxide is pumped into the ring reactor by a metering pump B. The synthesis process disclosed by the invention is less in methanol consumption, long in service life of the catalyst and simple in process device, realizes continuous operation, and can obtain relatively stable hydrogen peroxide conversion rate and relatively high epichlorohydrin selectivity in a long-time continuous operation process.
Description
Technical Field
The invention belongs to the field of catalytic synthesis, relates to a method for synthesizing epichlorohydrin, and more particularly relates to a continuous synthesis process of epichlorohydrin by a hydrogen peroxide method.
Background
Epichlorohydrin is an important organic chemical raw material and fine chemical products, and because molecules of epichlorohydrin contain active epoxy groups and chlorine atoms, the epichlorohydrin is quite active in chemical property, becomes an important basic organic chemical raw material and intermediate, and is widely used for synthesizing epoxy resin, glycerol, alcohol rubber, medicines, pesticides, surfactants, glass fiber reinforced plastics, ion exchange resin, coatings, plasticizers and the like.
At present, domestic and foreign researches mainly focus on a process for preparing epoxy chloropropane by directly epoxidizing chloropropene by using hydrogen peroxide as an oxygen source, and the process route does not generate salt-containing wastewater, only generates water through reaction, and has high atom utilization rate and small pollution. CN101124044A discloses a process for producing epichlorohydrin, which uses a titanium-silicon molecular sieve as a catalyst, uses methanol as a solvent, directly epoxidizes chloropropene to prepare epichlorohydrin, fills the titanium-silicon molecular sieve into a fixed bed, prepares chloropropene, methanol and hydrogen peroxide into a homogeneous phase, and pumps the homogeneous phase into the fixed bed at a certain temperature for reaction, wherein the reaction requires the preparation of the homogeneous phase for the feeding, so that a large amount of methanol is required to be used, and the recovery energy consumption of methanol is high. CN102093313A describes a method for preparing epichlorohydrin, which comprises feeding hydrogen peroxide, methanol, chloropropene and a catalyst into a reaction kettle for direct epoxidation, and performing membrane separation on the liquid-solid mixture after the reaction to obtain a solid part and a liquid part, wherein the solid part is the catalyst, and the liquid part is separated and refined to obtain epichlorohydrin. The catalyst of the process has short service time, the catalyst needs to be regenerated in each reaction, the process is complex, and the energy consumption is high.
Disclosure of Invention
The invention aims to overcome the defects in the synthesis process of the epichlorohydrin and provides the epichlorohydrin synthesis process which is low in methanol consumption, simple in process device and capable of realizing continuous operation by adopting a ring reactor.
The purpose of the invention is realized by the following technical scheme: the method is characterized in that the reactor is a ring reactor, the catalyst is pre-loaded in the ring reactor, chloropropene and methanol form chloropropene and methanol mixed liquor in a mixing tank, the chloropropene and methanol mixed liquor is pumped into the ring reactor by a metering pump A, and meanwhile, hydrogen peroxide is pumped into the ring reactor by a metering pump B.
The catalyst is TS-1 catalyst and is packed in 1 section or more than 1 section.
The loop reactor is also connected with other components, and the other components comprise a forced circulation pump, a mixer, a settling tank or centrifugal equipment, a sampling valve and a reaction liquid collecting tank.
The outlet of the loop reactor is also connected to a filter, preferably a ceramic filter.
The mol ratio of chloropropene to hydrogen peroxide is 1-4: 1.
The molar ratio of the methanol to the hydrogen peroxide is 1-5: 1.
The concentration of the hydrogen peroxide is 10-70%.
The reaction temperature is 0-80 ℃.
The residence time of the reactants in the loop reactor is 0.1-10 h.
The reaction pressure is 0-1 MPa.
The invention provides a continuous synthesis process of epoxy chloropropane by a hydrogen peroxide method, which adopts a ring reactor and has the following advantages: the continuous operation is realized, the safety of the reaction process is high, and the control is accurate; secondly, a large amount of methanol is not needed, and the recovery of the methanol is reduced; the service life of the catalyst is longer, and the catalyst does not need to be separated; and fourthly, the process device is simple and is convenient for realizing industrialization. The chloropropene is oxidized by adopting the method, and the stable oxidant conversion rate and the high target oxidation product selectivity can be obtained in the long-time continuous operation process. Particularly, the method has high epoxide selectivity, thereby reducing the difficulty of subsequent separation and purification.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention.
FIG. 1 is a flow chart of the continuous synthesis process of epichlorohydrin by hydrogen peroxide method.
Detailed Description
The following detailed description further describes the present invention for the purpose of illustrating the technical solutions and objects of the present invention.
The loop reactor of the invention uses jacket circulating water to control the temperature.
The forced circulation pump is positioned in the annular reactor, so that the catalyst is uniformly mixed with the chloropropene methanol mixed liquid and hydrogen peroxide.
The mixer is positioned between the metering pump and the inlet of the ring reactor and is used for uniformly mixing the chloropropene methanol mixed solution and hydrogen peroxide.
The settling tank or the centrifugal equipment is common or unusual equipment for settling or centrifuging, is positioned between the mixer and the inlet of the loop reactor, and is connected in series or in parallel by one or more than one stage to prevent mechanical impurities or particles in a reaction system from entering the loop reactor.
The filter of the present invention is connected to the outlet of the loop reactor to prevent the passage of the catalyst solids residue having the smallest particle size, resulting in catalyst loss.
The ring reactor of the invention is used for washing and activating the catalyst firstly, and has the specific operation that after the catalyst is filled in the reactor and the reactor is installed, deionized water is pumped in to fill the whole ring reactor, a circulating water bath is started, a forced circulating pump is started, deionized water is continuously injected into the reactor through a metering pump to wash and wet the catalyst, deionized water is drained, methanol is continuously injected into the reactor through the metering pump to wet and activate the catalyst, and methanol is drained.
[ example 1 ]
(1) Filling a TS-1 catalyst into a reactor according to the figure 1, filling sections I-III, installing the reactor, pumping deionized water to fill the whole loop reactor, starting a circulating water bath at the water temperature of 0 ℃, and starting a forced circulating pump. Injecting deionized water into the system continuously through a metering pump for 4 hours to wash the wet catalyst, and discharging the deionized water completely; and continuously injecting methanol into the system through a metering pump for 4 hours to wet and activate the catalyst, and discharging the methanol.
(2) Mixing chloropropene and methanol uniformly according to a molar ratio of 1: 1;
(3) meanwhile, a metering pump A, B is started, the mixer is fed with the materials, the mol ratio of chloropropene to hydrogen peroxide is controlled to be 1:1, and the solubility of hydrogen peroxide is controlled to be 50 wt%. Controlling the retention time of the materials in the ring reactor to be 2 hours;
(4) and measuring the hydrogen peroxide and gas spectrum of the produced material every 30min and quantifying until the content of the epichlorohydrin in the produced oil layer and the produced water layer reaches a stable value. And starting to stably run to realize continuous synthesis of the reaction.
(5) The operation was continued under the above-mentioned conditions, during which the composition of the reaction mixture output from the reactor was checked and the oxidant conversion, the epichlorohydrin selectivity, was calculated, wherein the results at reaction times of 2 hours, 500 hours, 1000 and 2000 hours are shown in table 1.
[ example 2 ]
(1) Filling a TS-1 catalyst into a reactor according to the figure 1, filling a section I, installing the reactor, pumping deionized water to fill the whole loop reactor, starting a circulating water bath at the water temperature of 10 ℃, and starting a forced circulating pump. Continuously injecting deionized water into the system through a metering pump for 6 hours to wash the wet catalyst, and discharging the deionized water; and continuously injecting methanol into the system through a metering pump for 8 hours to wet and activate the catalyst, and discharging the methanol.
(2) Mixing chloropropene and methanol uniformly according to a molar ratio of 2: 1;
(3) meanwhile, a metering pump A, B is started, the mixer is fed with the materials, the mol ratio of chloropropene to hydrogen peroxide is controlled to be 1:1, and the solubility of hydrogen peroxide is controlled to be 10 wt%. Controlling the retention time of the materials in the ring reactor to be 1 h;
(4) the same as in example 1.
(5) The same as in example 1.
[ example 3 ]
(1) Filling TS-1 catalyst into a reactor according to the figure 1, filling sections I-IV, installing the reactor, pumping deionized water to fill the whole loop reactor, starting a circulating water bath at the water temperature of 30 ℃, and starting a forced circulating pump. Injecting deionized water into the system continuously through a metering pump for 8 hours to wash the wet catalyst, and discharging the deionized water completely; and continuously injecting methanol into the system through a metering pump for 6 hours to wet and activate the catalyst, and discharging the methanol.
(2) Mixing chloropropene and methanol uniformly according to a molar ratio of 1: 1;
(3) meanwhile, a metering pump A, B is started, the mixer is fed with the materials, the mol ratio of chloropropene to hydrogen peroxide is controlled to be 3:1, and the solubility of hydrogen peroxide is controlled to be 70 wt%. Controlling the retention time of the materials in the ring reactor to be 0.1 h;
(4) the same as in example 1.
(5) The same as in example 1.
[ example 4 ]
(1) Filling a TS-1 catalyst into a reactor according to the figure 1, filling sections I and II, installing the reactor, pumping deionized water to fill the whole loop reactor, starting a circulating water bath at the water temperature of 80 ℃, and starting a forced circulating pump. Injecting deionized water into the system continuously through a metering pump for 10 hours to wash the wet catalyst, and discharging the deionized water completely; and continuously injecting methanol into the system through a metering pump for 24 hours to wet and activate the catalyst, and discharging the methanol.
(2) Mixing chloropropene and methanol uniformly according to a molar ratio of 5: 1;
(3) meanwhile, a metering pump A, B is started, the mixer is fed with the materials, the mol ratio of chloropropene to hydrogen peroxide is controlled to be 2:1, and the solubility of hydrogen peroxide is controlled to be 70 wt%. Controlling the retention time of the materials in the loop reactor to be 10 h;
(4) the same as in example 1.
(5) The same as in example 1.
[ example 5 ]
(1) Filling TS-1 catalyst into a reactor according to the figure 1, filling sections I-IV, installing the reactor, pumping deionized water to fill the whole loop reactor, starting a circulating water bath at the water temperature of 20 ℃, and starting a forced circulating pump. Injecting deionized water into the system continuously through a metering pump for 10 hours to wash the wet catalyst, and discharging the deionized water completely; and continuously injecting methanol into the system through a metering pump for 12h to wet and activate the catalyst, and discharging the methanol.
(2) Mixing chloropropene and methanol uniformly according to a molar ratio of 4: 3;
(3) meanwhile, a metering pump A, B is started, the mixer is fed with the materials, the mol ratio of chloropropene to hydrogen peroxide is controlled to be 4:1,
the solubility of hydrogen peroxide is 40 wt%. Controlling the retention time of the materials in the ring reactor to be 3 h;
(4) the same as in example 1.
(5) The same as in example 1.
[ example 6 ]
(1) Filling TS-1 catalyst into a reactor according to the figure 1, filling sections I-IV, installing the reactor, pumping deionized water to fill the whole loop reactor, starting a circulating water bath at the water temperature of 10 ℃, and starting a forced circulating pump. Injecting deionized water into the system continuously through a metering pump for 12 hours to wash the wet catalyst, and discharging the deionized water completely; and continuously injecting methanol into the system through a metering pump for 16h to wet and activate the catalyst, and discharging the methanol.
(2) Mixing chloropropene and methanol uniformly according to a molar ratio of 3: 5;
(3) meanwhile, a metering pump A, B is started, the mixer is fed with the materials, the mol ratio of chloropropene to hydrogen peroxide is controlled to be 3:1,
the solubility of hydrogen peroxide is 60 wt%. Controlling the retention time of the materials in the ring reactor to be 1 h;
(4) the same as in example 1.
(5) The same as in example 1.
Table 1 examples 1-6 continuous run results data
Comparative example 1
(1) Chloropropene, methanol, hydrogen peroxide and a catalyst in the same proportion as in example 5 are added into a reaction kettle, the temperature is raised to 42 ℃, and the reaction is carried out for 2 h.
(2) And (4) after the reaction is finished, detecting the hydrogen peroxide residue and the content of epoxy chloropropane in the reaction solution, and calculating the hydrogen peroxide conversion rate and the yield of the epoxy chloropropane. The catalyst is used for next batch of epoxidation reaction after being filtered.
The results are listed in table 2.
Table 2 data of catalyst application results of comparative examples
The invention is not limited to the embodiments of the invention described.
The structure and the implementation of the present invention are described herein by using specific examples, and the above description of the examples is only used to help understand the core idea of the present invention. It should be noted that, for those skilled in the art, it is possible to make various improvements and modifications to the present invention without departing from the principle of the present invention, and those improvements and modifications also fall within the scope of the claims of the present invention.
Claims (10)
1. A continuous synthesis process of epoxy chloropropane by hydrogen peroxide is characterized in that hydrogen peroxide, methanol, chloropropene and a catalyst are put into a reactor for epoxidation, the reactor is a ring reactor, the catalyst is pre-loaded into the ring reactor, chloropropene and methanol form a chloropropene-methanol mixed solution in a mixing tank, the chloropropene-methanol mixed solution is pumped into the ring reactor by a metering pump A, and hydrogen peroxide is pumped into the ring reactor by a metering pump B.
2. The continuous synthesis process of epichlorohydrin by hydrogen peroxide method according to claim 1, wherein the catalyst is a TS-1 catalyst and is packed in 1 or more stages.
3. The continuous synthesis process of epichlorohydrin by hydrogen peroxide method according to claim 1, wherein the loop reactor is further connected with other components, and the other components comprise a forced circulation pump, a mixer, a settling tank or a centrifugal device, a production valve and a reaction liquid collecting tank.
4. The continuous synthesis process of epichlorohydrin by hydrogen peroxide method according to claim 3, wherein the outlet of the loop reactor is further connected with a filter, preferably a ceramic filter.
5. The continuous synthesis process of epoxy chloropropane by using a hydrogen peroxide method according to claim 1, characterized in that the molar ratio of chloropropene to hydrogen peroxide is 1-4: 1.
6. The continuous synthesis process of epichlorohydrin by a hydrogen peroxide method according to claim 1, wherein the molar ratio of methanol to hydrogen peroxide is 1-5: 1.
7. The continuous synthesis process of epichlorohydrin by using hydrogen peroxide as claimed in claim 1, wherein the concentration of hydrogen peroxide is 10-70%.
8. The process for the continuous synthesis of epichlorohydrin by hydrogen peroxide method according to claim 1, wherein the reaction temperature is 0-80 ℃.
9. The continuous synthesis process of epichlorohydrin by hydrogen peroxide method according to claim 1, wherein the residence time of the reactants in the loop reactor is 0.1-10 h.
10. The process for continuously synthesizing epichlorohydrin by a hydrogen peroxide method according to claim 1, wherein the reaction pressure is 0-1 MPa.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010992565.8A CN111978273A (en) | 2020-09-21 | 2020-09-21 | Continuous synthesis process of epoxy chloropropane by hydrogen peroxide method |
| KR1020237013755A KR20230092922A (en) | 2020-09-21 | 2021-09-18 | Continuous synthesis process of epichlorohydrin and continuous reaction device |
| PCT/CN2021/119424 WO2022057931A1 (en) | 2020-09-21 | 2021-09-18 | Continuous synthesis process and continuous reaction device for epichlorohydrin |
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| CN202010992565.8A CN111978273A (en) | 2020-09-21 | 2020-09-21 | Continuous synthesis process of epoxy chloropropane by hydrogen peroxide method |
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| KR (1) | KR20230092922A (en) |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2022057931A1 (en) * | 2020-09-21 | 2022-03-24 | 江苏扬农化工集团有限公司 | Continuous synthesis process and continuous reaction device for epichlorohydrin |
| CN116514741A (en) * | 2023-07-04 | 2023-08-01 | 山东民基新材料科技有限公司 | Process for producing epoxy chloropropane by utilizing micro-interface reaction |
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2020
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- 2021-09-18 KR KR1020237013755A patent/KR20230092922A/en active Search and Examination
- 2021-09-18 WO PCT/CN2021/119424 patent/WO2022057931A1/en active Application Filing
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| WO2022057931A1 (en) * | 2020-09-21 | 2022-03-24 | 江苏扬农化工集团有限公司 | Continuous synthesis process and continuous reaction device for epichlorohydrin |
| CN116514741A (en) * | 2023-07-04 | 2023-08-01 | 山东民基新材料科技有限公司 | Process for producing epoxy chloropropane by utilizing micro-interface reaction |
| CN116514741B (en) * | 2023-07-04 | 2023-09-26 | 山东民基新材料科技有限公司 | Process for producing epoxy chloropropane by utilizing micro-interface reaction |
Also Published As
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| KR20230092922A (en) | 2023-06-26 |
| WO2022057931A1 (en) | 2022-03-24 |
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