CN1769277A - Epichlorohydrin production process - Google Patents
Epichlorohydrin production process Download PDFInfo
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- CN1769277A CN1769277A CN 200510032373 CN200510032373A CN1769277A CN 1769277 A CN1769277 A CN 1769277A CN 200510032373 CN200510032373 CN 200510032373 CN 200510032373 A CN200510032373 A CN 200510032373A CN 1769277 A CN1769277 A CN 1769277A
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- propenyl chloride
- hydrogen peroxide
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- BRLQWZUYTZBJKN-UHFFFAOYSA-N Epichlorohydrin Chemical compound ClCC1CO1 BRLQWZUYTZBJKN-UHFFFAOYSA-N 0.000 title claims abstract description 16
- 238000004519 manufacturing process Methods 0.000 title claims description 27
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims abstract description 72
- OWXJKYNZGFSVRC-NSCUHMNNSA-N (e)-1-chloroprop-1-ene Chemical compound C\C=C\Cl OWXJKYNZGFSVRC-NSCUHMNNSA-N 0.000 claims abstract description 46
- 239000003054 catalyst Substances 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims abstract description 15
- 239000007791 liquid phase Substances 0.000 claims abstract description 15
- 239000000463 material Substances 0.000 claims abstract description 14
- 238000006735 epoxidation reaction Methods 0.000 claims abstract description 13
- 239000002002 slurry Substances 0.000 claims abstract description 12
- UGACIEPFGXRWCH-UHFFFAOYSA-N [Si].[Ti] Chemical compound [Si].[Ti] UGACIEPFGXRWCH-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000012071 phase Substances 0.000 claims abstract description 7
- 239000002808 molecular sieve Substances 0.000 claims abstract description 6
- 238000007670 refining Methods 0.000 claims abstract description 6
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 6
- LRWZZZWJMFNZIK-UHFFFAOYSA-N 2-chloro-3-methyloxirane Chemical compound CC1OC1Cl LRWZZZWJMFNZIK-UHFFFAOYSA-N 0.000 claims description 16
- 239000002904 solvent Substances 0.000 claims description 7
- 239000002994 raw material Substances 0.000 claims description 6
- 230000004087 circulation Effects 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 239000013078 crystal Substances 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 21
- 238000006243 chemical reaction Methods 0.000 description 13
- 238000005516 engineering process Methods 0.000 description 8
- 239000000047 product Substances 0.000 description 6
- 230000007797 corrosion Effects 0.000 description 5
- 238000005260 corrosion Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 238000006555 catalytic reaction Methods 0.000 description 3
- 238000005660 chlorination reaction Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 150000002924 oxiranes Chemical class 0.000 description 3
- 238000006276 transfer reaction Methods 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 2
- AVXURJPOCDRRFD-UHFFFAOYSA-N Hydroxylamine Chemical compound ON AVXURJPOCDRRFD-UHFFFAOYSA-N 0.000 description 2
- MLHOXUWWKVQEJB-UHFFFAOYSA-N Propyleneglycol diacetate Chemical compound CC(=O)OC(C)COC(C)=O MLHOXUWWKVQEJB-UHFFFAOYSA-N 0.000 description 2
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 235000019628 coolness Nutrition 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000007363 ring formation reaction Methods 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000010703 silicon 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
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 239000004593 Epoxy Substances 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 1
- 239000004902 Softening Agent Substances 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- HQABUPZFAYXKJW-UHFFFAOYSA-N butan-1-amine Chemical compound CCCCN HQABUPZFAYXKJW-UHFFFAOYSA-N 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 125000001309 chloro group Chemical group Cl* 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 125000003700 epoxy group Chemical group 0.000 description 1
- 239000003822 epoxy resin Substances 0.000 description 1
- 230000005669 field effect Effects 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 235000011187 glycerol Nutrition 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- SYECJBOWSGTPLU-UHFFFAOYSA-N hexane-1,1-diamine Chemical compound CCCCCC(N)N SYECJBOWSGTPLU-UHFFFAOYSA-N 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003701 inert diluent Substances 0.000 description 1
- 150000002484 inorganic compounds Chemical class 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000000543 intermediate Substances 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 150000007530 organic bases Chemical class 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 229920000647 polyepoxide Polymers 0.000 description 1
- 230000003014 reinforcing effect Effects 0.000 description 1
- 238000007142 ring opening reaction Methods 0.000 description 1
- 239000005060 rubber Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000009987 spinning Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001839 systemic circulation Effects 0.000 description 1
- OSBSFAARYOCBHB-UHFFFAOYSA-N tetrapropylammonium Chemical compound CCC[N+](CCC)(CCC)CCC OSBSFAARYOCBHB-UHFFFAOYSA-N 0.000 description 1
- LPSKDVINWQNWFE-UHFFFAOYSA-M tetrapropylazanium;hydroxide Chemical compound [OH-].CCC[N+](CCC)(CCC)CCC LPSKDVINWQNWFE-UHFFFAOYSA-M 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- XJDNKRIXUMDJCW-UHFFFAOYSA-J titanium tetrachloride Chemical compound Cl[Ti](Cl)(Cl)Cl XJDNKRIXUMDJCW-UHFFFAOYSA-J 0.000 description 1
- XROWMBWRMNHXMF-UHFFFAOYSA-J titanium tetrafluoride Chemical compound [F-].[F-].[F-].[F-].[Ti+4] XROWMBWRMNHXMF-UHFFFAOYSA-J 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Abstract
The invention discloses a process for producing epichlorohydrin, which comprises proportioning chloropropene and titanium-silicon molecular sieve catalyst, charging into helical channel type revolving beds or rotary filling bed hypergravity reactor, continuously charging liquid phase or gas phase chloropropene and hydrogen peroxide solution simultaneously for direct epoxidation reaction, the non-reacted chloropropene and a small amount of produced gas condensating and returning proportioning tank for continuing use, the slurry in the reactor flowing into the proportioning tank, pressurizing part of the materials and circulating into the reactor, loading part of the materials into separator, loading the separated crude epichlorohydrin for refining, and returning slurry containing catalyst to proportioning tank for later use again.
Description
One, technical field
The present invention relates to a kind of epichlorohydrin production process, specifically, relate to by propenyl chloride and hydrogen peroxide under the super gravity field effect directly catalysis epoxidation produce the technology of epoxy chloropropane.
Two, background technology
Epoxy chloropropane is a kind of important basic Organic Chemicals and intermediate, epoxy chloropropane is owing to contain active epoxy group(ing) and chlorine atom in its molecule, being widely used in synthetic epoxy resin, glycerine, ammonia hydrin rubber, medicine, agricultural chemicals, tensio-active agent, ion exchange resin and softening agent etc., is the third-largest epoxy compounds that output is only second to oxyethane and propylene oxide.At present, epoxy chloropropane is raw material production with the propylene, and production technique mainly contains propylene high-temperature chlorination process and propylene acetate method.The propylene high-temperature chlorination process is the main method of industrial production epoxy chloropropane, technical maturity, and production process is flexible.But there are some serious defectives in this production technique, and many as by product, energy consumption is big, and equipment corrosion is serious, the equipment maintenance cost height, and production process produces a large amount of calcium chloride (CaCl that contain
2) and the waste water of organochlorine, the serious harm environment, the investment of administering waste water accounts for the 15%-20% of gross investment, thereby causes the production cost of epoxy chloropropane to raise significantly.The propylene acetate method is compared with the propylene high-temperature chlorination process, material consumption, energy consumption, amount of by-products and wastewater flow rate all have decline in various degree, but technical process is longer, the problem of equipment corrosion and a large amount of discharge of wastewater does not still solve, and the expense of the maintenance of the equipment and the disposal of three wastes has still surpassed 10% of gross investment.
In order to solve corrosion and the environmental issue in the epoxy chloropropane production process effectively, US4,833,260 disclose a kind of is catalyzer with the HTS, directly alkene (comprising haloolefin) is carried out the production technique that epoxidation is produced epoxide with hydrogen peroxide.Because have strong polar compound such as water or alcohol in the reaction system, the catalysis ring-opening reaction will partly take place in the epoxide of generation, reduce the yield of epoxide.For this reason, US4,824,976, CN1319099 and CN1131152A disclose some and improved the assist measure of epoxidised yield, as added alkaline organic or inorganic compound etc.In addition, this class exothermic heat of reaction is bigger, and heat-obtaining is untimely, easy temperature runaway, the invalid rate of decomposition of increase hydrogen peroxide, therefore, CN1219536A slows down reaction by add solid inert diluents in catalyzer, be beneficial to temperature control, but the useful volume of reactor descends obviously.EP0659473A1 discloses a kind of trickle-bed reactor and production technique thereof that is used for chloro propylene epoxidation, this reactor structure complexity, the working pressure height, temperature control relies on the systemic circulation material and realizes, needing also after reaction finishes that solvent is evaporated separation recycles with realization, therefore, energy consumption is very high.In addition, granules of catalyst is too big, has increased diffusional resistance, has reduced the effective rate of utilization of catalyzer.CN1534030A discloses a kind of epichlorohydrin production process, and propenyl chloride, hydrogen peroxide, solvent and titanium-silicon molecular sieve catalyst fine particle carry out epoxidation reaction in tank reactor.This production technique adopts the direct epoxidation of hydrogen peroxide, can solve corrosion and pollution problem that chlorohydrination technology exists, but the reactor volume is big, and the reactor useful volume is little, and flow process is longer, invests still higherly, is unfavorable for the production of epoxy chloropropane.
Produce investment in order to reduce, CN2581060A discloses a kind of structural shape of reactor, and CN1059105A discloses the structural shape of another reactor.The front is a kind of to be the rotating bed with helix channel supergravity reactor, and the back is a kind of to be the rotating packed bed supergravity reactor.Two-phase or multiphase logistics can be in these two kinds of supergravity reactors adverse current or and the stream contact carry out mass transfer or mass transfer-reaction, these two kinds of supergravity reactors can both reinforcing mass transfer process or mass transfer-reaction process.
Three, summary of the invention
The purpose of this invention is to provide a kind of epichlorohydrin production process, just provide a kind of flow process is simple, energy consumption the is low direct epoxidation of propenyl chloride to prepare the technology of epoxy chloropropane on the basis of existing technology.
Epichlorohydrin production process: after liquid phase propenyl chloride and titanium-silicon molecular sieve catalyst configured, add supergravity reactor from the liquid phase feeding mouth, hydrogen peroxide enters reactor by another one liquid phase feeding mouth.Propenyl chloride can liquid phase or the gas phase form enter supergravity reactor, in reactor, carry out epoxidation reaction with hydrogen peroxide.A small amount of gas of unreacted propenyl chloride and generation returns material-compound tank through condensation to be continued to use, slurries in the reactor flow into material-compound tank, reactor is squeezed in partial material circulation after the pump pressurization, partial material is sent separator, thick epoxy chloropropane after the separation is sent to refining, and the slurries that contain catalyzer return material-compound tank to be continued to use.
Technology provided by the invention comprises: propenyl chloride, hydrogen peroxide and titanium-silicon molecular sieve catalyst fine particle react by supergravity reactor, a small amount of gas of unreacted propenyl chloride and generation returns material-compound tank through condensation to be continued to use, slurries in the reactor flow into material-compound tank, reactor is squeezed in partial material circulation after the pump pressurization, partial material is sent separator, thick epoxy chloropropane after the separation is sent to refining, and the concentrated slurry that contains catalyzer returns material-compound tank to be continued to use.The concentration of the concentration ratio hydrogen peroxide of propenyl chloride is high 1 to 2 times in the reactor.
Described hydrogen peroxide can be pure product, in order to keep the safety in production, considers economic factors simultaneously, preferably uses the aqueous solution of hydrogen peroxide, and its concentration is selected from 5%～90%, and the present invention selects industrial common concentration 27.5%.
Described HTS is with inorganic titanium source such as titanous chloride (TiCl
3), titanium tetrachloride (TiCl
4) and titanium tetrafluoride (TiF
4) wait and be raw material, silicon sol is as the silicon source, use ammoniacal liquor (or organic bases such as hexanediamine, n-Butyl Amine 99, tetrapropyl oxyammonia) to be alkali source, with a spot of tetrapropyl amine bromide (TPABr) or tetrapropyl oxyammonia (TPAOH) as template, prepare glue, the big crystallite titanium-silicon molecular sieve that hydrothermal crystallizing makes in autoclave then earlier.The synthetic cost of this catalyzer is low, is used for catalyzed reaction and is easy to product and catalyst separating.
Positively effect of the present invention is: because the reactor that adopts is rotating bed with helix channel supergravity reactor or rotating packed bed supergravity reactor, though in reaction system, do not add any solvent, but under the hypergravity effect, immiscible propenyl chloride also can contact closely with hydrogen peroxide, can strengthen the mass transfer-reaction process of propenyl chloride and hydrogen peroxide epoxidation reaction, guarantee to react and carry out fast, can realize the direct epoxidation continuous production of propenyl chloride and hydrogen peroxide, improve the hydrogen peroxide utilization ratio, cut down the consumption of energy, reduce investment outlay, heavy corrosion and pollution problem that chlorohydrination technology exists can have fundamentally been solved, because solubilizing agent not, can also a large amount of economy system working costs, reduce production costs.Technical process of the present invention is simple, the reaction conditions gentleness, and mass-and heat-transfer is effective, and reactor throughput is big, adopts the HTS of big crystal grain, helps product and catalyst separating, adopts the spinning liquid isolation technique, has simplified the separating technology of catalyzer.
Four, description of drawings
Five, embodiment
Below in conjunction with accompanying drawing production technique provided by the present invention is further detailed, but not thereby limiting the invention.
When producing epoxy chloropropane in gas phase propenyl chloride mode, in material-compound tank 4, catalyst raw powder and liquid phase propenyl chloride are disposed in proportion, after mixing to a certain degree, with pump 5 mixture is squeezed into supergravity reactor 2, another one liquid phase feeding mouth by reactor feeds hydrogen peroxide, continuously propenyl chloride is fed reactor through well heater 1 heating back from the gas-phase feed mouth by a certain percentage simultaneously, gas propenyl chloride and hydrogen peroxide carry out cyclization in reactor.Temperature of reaction is 50 ℃～80 ℃, and preferred 60 ℃～70 ℃, the reaction absolute pressure is 0.1MPa～0.5MPa, preferred 0.1MPa～0.3MPa.A small amount of gas of unreacted propenyl chloride and generation enters condenser 3 coolings, non-condensable gas emptying, and phlegma returns material-compound tank.Slurries in the reactor flow into material-compound tank, and reactor is squeezed in partial material circulation after pump 5 pressurizations, and partial material is sent separator 6, and the concentrated slurry that contains catalyzer returns material-compound tank to be continued to use, and thick epoxy chloropropane product is sent to refining and solvent recuperation.
When producing epoxy chloropropane in liquid phase propenyl chloride mode, in material-compound tank 4, catalyst raw powder and liquid phase propenyl chloride are disposed in proportion, after mixing to a certain degree, with pump 5 mixture is squeezed into supergravity reactor 2, continuously hydrogen peroxide and liquid phase propenyl chloride are fed reactor by a certain percentage, propenyl chloride and hydrogen peroxide carry out cyclization in reactor.Temperature of reaction is 35 ℃～60 ℃, and preferred 40 ℃～50 ℃, the reaction absolute pressure is 0.1MPa～0.5MPa, preferred 0.1MPa～0.3MPa.A small amount of gas of unreacted propenyl chloride and generation enters condenser 3 coolings, non-condensable gas emptying, and phlegma returns material-compound tank.Slurries in the reactor flow into material-compound tank, and reactor is squeezed in partial material circulation after pump 5 pressurizations, and partial material is sent separator 6, and the concentrated slurry that contains catalyzer returns material-compound tank to be continued to use, and thick epoxy chloropropane product is sent to refining and solvent recuperation.
To the present invention's further instruction in addition, but therefore do not limit the present invention below by example.
Catalyzer is a HTS, and the grain graininess scope is 200 μ m～0.5 μ m, and reaction raw materials is 27.5% industrial hydrogen peroxide and the industrial propenyl chloride of content more than 97%.Catalyst levels is 1% of a propenyl chloride weight, is warmed up to 45 ℃ under normal pressure, and 2: 1 in molar ratio ratio adds propenyl chloride and hydrogen peroxide, the mass space velocity 2.0h of propenyl chloride
-1Result: hydrogen peroxide transformation efficiency 100%, the epoxidised selectivity 95.5% of hydrogen peroxide.
Catalyzer is a HTS, and the grain graininess scope is 200 μ m～0.5 μ m, and reaction raw materials is 27.5% industrial hydrogen peroxide and the industrial propenyl chloride of content more than 97%.Catalyst levels is 1% of a propenyl chloride weight, is warmed up to 65 ℃ under normal pressure, and 2: 1 in molar ratio ratio adds propenyl chloride and hydrogen peroxide, the mass space velocity 2.5h of propenyl chloride
-1The vapour-liquid ratio of charging is 1.5～6: 1.Result: hydrogen peroxide transformation efficiency 100%, the epoxidised selectivity 95% of hydrogen peroxide.
Catalyzer is a HTS, and the grain graininess scope is 200 μ m～0.5 μ m, and reaction raw materials is 27.5% industrial hydrogen peroxide and the industrial propenyl chloride of content more than 97%.Catalyst levels is 1% of a propenyl chloride weight, is warmed up to 60 ℃ under the pressure (absolute pressure) of 0.15MPa, and 2: 1 in molar ratio ratio adds propenyl chloride and hydrogen peroxide, the mass space velocity 1.5h of propenyl chloride.The vapour-liquid ratio of charging is 1.5～6: 1.Result: hydrogen peroxide transformation efficiency 100%, the epoxidised selectivity 96% of hydrogen peroxide.
Claims (6)
1. epichlorohydrin production process, it is characterized in that: liquid phase propenyl chloride and titanium-silicon molecular sieve catalyst are configured back adding supergravity reactor, add liquid phase or gas phase propenyl chloride and hydrogen peroxide simultaneously continuously, propenyl chloride and hydrogen peroxide directly carry out epoxidation reaction under katalysis, a small amount of gas of unreacted propenyl chloride and generation returns material-compound tank through condensation to be continued to use, slurries in the reactor flow into material-compound tank, partial material pressurization back circulation enters reactor, partial material is sent separator, thick epoxy chloropropane after the separation is sent to refining, and the slurries that contain catalyzer return material-compound tank to be continued to use.
2. epichlorohydrin production process according to claim 1 is characterized in that reactor used be helical channel rotating bed pattern or rotating packed bed pattern supergravity reactor.
3. epichlorohydrin production process according to claim 1 is characterized in that propenyl chloride and hydrogen peroxide directly carry out epoxidation reaction under katalysis, can not add solvent.
4. epichlorohydrin production process according to claim 1, it is characterized in that propenyl chloride can liquid phase or the gas phase form add supergravity reactor, in reactor, carry out quick epoxidation reaction with hydrogen peroxide.
5. epichlorohydrin production process according to claim 1 is characterized in that catalyzer is the HTS of the big crystal grain of inorganic titanium silicon raw material synthetic, and its size range is 200 μ m～0.5 μ m.
6. epichlorohydrin production process according to claim 1 is characterized in that catalyst levels is 0.2%～3% (weight) of propenyl chloride.
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|---|---|---|---|
| CN 200510032373 CN1769277A (en) | 2005-11-14 | 2005-11-14 | Epichlorohydrin production process |
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|---|---|---|---|
| CN 200510032373 CN1769277A (en) | 2005-11-14 | 2005-11-14 | Epichlorohydrin production process |
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101434586B (en) * | 2007-11-15 | 2012-07-18 | 中国石油化工股份有限公司 | Propylene chloride epoxidation process in the presence of hydrogen and oxygen |
| TWI427072B (en) * | 2008-03-17 | 2014-02-21 | Momentive Specialty Chem Inc | Process for the preparation of epichlorohydrin |
| US8735614B2 (en) | 2011-01-27 | 2014-05-27 | Solvay Sa | Process for the manufacture of 1,2-epoxy-3-chloropropane |
| US8796478B2 (en) | 2011-01-27 | 2014-08-05 | Solvay Sa | Process for the manufacture of 1,2-epoxy-3-chloropropane |
| CN112625008A (en) * | 2020-12-25 | 2021-04-09 | 北京化工大学 | System and method for preparing epichlorohydrin |
| CN113527037A (en) * | 2021-08-20 | 2021-10-22 | 浙江迪邦化工有限公司 | Method for continuously producing chloroethane by using supergravity reactor |
| CN113856407A (en) * | 2021-10-28 | 2021-12-31 | 山东新龙集团有限公司 | Method for treating tail gas in process of preparing epoxy chloropropane by oxidation method |
| CN115646391A (en) * | 2022-11-03 | 2023-01-31 | 重庆市化工研究院有限公司 | Synthesis device and method of vinyl pivalate |
| CN115888354A (en) * | 2021-08-19 | 2023-04-04 | 中国石油化工股份有限公司 | Device and method for removing oxygen in tail gas of epoxypropane process |
| CN116174030A (en) * | 2023-01-04 | 2023-05-30 | 万华化学集团股份有限公司 | A surface-modified silicate titanium-silicon molecular sieve catalyst and its preparation method and its application in the preparation of epichlorohydrin by epoxidation |
| CN116199649A (en) * | 2022-12-13 | 2023-06-02 | 江西师范大学 | A method and device for producing epichlorohydrin using a loaded TS-2 molecular sieve fixed bed reactor |
| CN116217518A (en) * | 2023-02-07 | 2023-06-06 | 华陆工程科技有限责任公司 | Production method and production device of epoxy chloropropane |
| 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 |
-
2005
- 2005-11-14 CN CN 200510032373 patent/CN1769277A/en active Pending
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101434586B (en) * | 2007-11-15 | 2012-07-18 | 中国石油化工股份有限公司 | Propylene chloride epoxidation process in the presence of hydrogen and oxygen |
| TWI427072B (en) * | 2008-03-17 | 2014-02-21 | Momentive Specialty Chem Inc | Process for the preparation of epichlorohydrin |
| US8735614B2 (en) | 2011-01-27 | 2014-05-27 | Solvay Sa | Process for the manufacture of 1,2-epoxy-3-chloropropane |
| US8796478B2 (en) | 2011-01-27 | 2014-08-05 | Solvay Sa | Process for the manufacture of 1,2-epoxy-3-chloropropane |
| CN112625008B (en) * | 2020-12-25 | 2022-07-15 | 北京化工大学 | A kind of preparation system and method of epichlorohydrin |
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