CN112500371A - Etherification-free system and process for preparing propylene oxide by virtue of intensified propylene epoxidation - Google Patents
Etherification-free system and process for preparing propylene oxide by virtue of intensified propylene epoxidation Download PDFInfo
- Publication number
- CN112500371A CN112500371A CN201910867736.1A CN201910867736A CN112500371A CN 112500371 A CN112500371 A CN 112500371A CN 201910867736 A CN201910867736 A CN 201910867736A CN 112500371 A CN112500371 A CN 112500371A
- Authority
- CN
- China
- Prior art keywords
- propylene
- reaction zone
- reaction
- epoxidation
- micro
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 191
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 190
- 238000006735 epoxidation reaction Methods 0.000 title claims abstract description 113
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 24
- 238000006243 chemical reaction Methods 0.000 claims description 224
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 82
- 239000011259 mixed solution Substances 0.000 claims description 60
- 239000007788 liquid Substances 0.000 claims description 57
- WEVYAHXRMPXWCK-UHFFFAOYSA-N Acetonitrile Chemical compound CC#N WEVYAHXRMPXWCK-UHFFFAOYSA-N 0.000 claims description 48
- 239000007789 gas Substances 0.000 claims description 31
- 238000000926 separation method Methods 0.000 claims description 30
- 238000003860 storage Methods 0.000 claims description 29
- 239000000047 product Substances 0.000 claims description 22
- 239000003054 catalyst Substances 0.000 claims description 17
- 239000012046 mixed solvent Substances 0.000 claims description 16
- 239000007795 chemical reaction product Substances 0.000 claims description 15
- 238000006266 etherification reaction Methods 0.000 claims description 5
- 238000009835 boiling Methods 0.000 claims description 3
- 239000000243 solution Substances 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 23
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 abstract description 18
- 230000007797 corrosion Effects 0.000 abstract description 8
- 238000005260 corrosion Methods 0.000 abstract description 8
- 230000000694 effects Effects 0.000 abstract description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 6
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 6
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 4
- 239000001282 iso-butane Substances 0.000 description 4
- 235000013847 iso-butane Nutrition 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- -1 polypropylene Polymers 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 3
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 3
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 239000000010 aprotic solvent Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000003139 buffering effect Effects 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- XENVCRGQTABGKY-ZHACJKMWSA-N chlorohydrin Chemical compound CC#CC#CC#CC#C\C=C\C(Cl)CO XENVCRGQTABGKY-ZHACJKMWSA-N 0.000 description 2
- 235000019441 ethanol Nutrition 0.000 description 2
- JRNXSPIOMZDAQR-UHFFFAOYSA-N ethylperoxybenzene Chemical compound CCOOC1=CC=CC=C1 JRNXSPIOMZDAQR-UHFFFAOYSA-N 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000007142 ring opening reaction Methods 0.000 description 2
- 238000005728 strengthening Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- RZWHKKIXMPLQEM-UHFFFAOYSA-N 1-chloropropan-1-ol Chemical compound CCC(O)Cl RZWHKKIXMPLQEM-UHFFFAOYSA-N 0.000 description 1
- RNDNSYIPLPAXAZ-UHFFFAOYSA-N 2-Phenyl-1-propanol Chemical compound OCC(C)C1=CC=CC=C1 RNDNSYIPLPAXAZ-UHFFFAOYSA-N 0.000 description 1
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 1
- 241001292396 Cirrhitidae Species 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- 241000208125 Nicotiana Species 0.000 description 1
- 235000002637 Nicotiana tabacum Nutrition 0.000 description 1
- 239000004721 Polyphenylene oxide Substances 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 150000001722 carbon compounds Chemical class 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000003995 emulsifying agent Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000002736 nonionic surfactant Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 229920000570 polyether Polymers 0.000 description 1
- 229920005862 polyol Polymers 0.000 description 1
- 150000003077 polyols Chemical class 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000007127 saponification reaction Methods 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 239000000080 wetting agent 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
- C07D303/04—Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Epoxy Compounds (AREA)
Abstract
The invention provides an etherification-free system and process for preparing propylene oxide by the epoxidation of reinforced propylene, which relate to the technical field of preparing propylene oxide by the epoxidation of propylene and comprise the following steps: the etherification-free system and the etherification-free process for preparing propylene oxide by the epoxidation of propylene are enhanced, and the etherification-free system and the etherification-free process for preparing propylene oxide achieve the effects of no equipment corrosion and no generation of ether products in the process of preparing propylene oxide.
Description
Technical Field
The invention relates to the technical field of propylene epoxide preparation by propylene epoxidation, in particular to an etherification-free system and process for preparing propylene epoxide by propylene epoxidation.
Background
Propylene Oxide (PO) is the third largest organic chemical product among propylene derivatives that has a second yield to polypropylene and acrylonitrile. The epoxy propane has wide application, and can be used for producing propylene glycol, nonionic surfactant, oil field demulsifier, pesticide emulsifier, wetting agent and the like besides polyether polyol and glycerol. The derivative of the epoxypropane is also widely used in the industries of automobiles, buildings, foods, tobacco, medicines, cosmetics and the like. With the expansion of propylene oxide use and the increasing use of downstream products, the demand for propylene oxide in the market has increased year by year.
Currently, the main processes for the industrial production of propylene oxide are the chlorohydrin process and the co-oxidation process (also known as the indirect oxidation process, or Halcon process), which account for more than about 99% of the total world production capacity. The chlorohydrin method is to react propylene with chlorine and water to generate chloropropanol, and then to perform saponification reaction under the action of alkali liquor to obtain propylene oxide. This method has been the main method of producing PO since the 30 s of the 20 th century since its development and industrial production by united states carbon compounds corporation. The co-oxidation process is divided into the iso-butane process and the ethylbenzene process. Isobutane (or ethylbenzene) is oxidized to generate isobutane peroxide (or ethylbenzene peroxide), and then the isobutane peroxide (or ethylbenzene peroxide) reacts with propylene to generate PO, and simultaneously, tert-butyl alcohol (or alpha-methyl phenyl ethyl alcohol) is co-produced.
However, in the process of producing propylene oxide by using a chlorohydrination method, a large amount of salt-containing wastewater and organic chloride are generated, so that equipment corrosion and pollution discharge are serious, and in the process of producing propylene oxide by using a co-oxidation method, the defects of pollution, corrosion, chlorine resource requirement and the like of the chlorohydrination method can be overcome, but the process is long, the investment is large, ether products are easily generated, and the production cost is increased.
Disclosure of Invention
In view of this, the invention provides an etherification-free system and process for preparing propylene oxide by the enhanced epoxidation of propylene, so as to achieve the effects of no equipment corrosion and no generation of ether products in the process of preparing propylene oxide.
The technical purpose of the invention is realized by the following technical scheme.
An etherification-free system for the enhanced epoxidation of propylene to propylene oxide comprising:
a propylene storage tank for storing and transporting propylene;
the mixed solvent storage tank is used for preparing and conveying mixed liquid of hydrogen peroxide, acetonitrile and a catalyst;
the gas-liquid separator is used for receiving the propylene epoxidation product and carrying out gas-liquid separation on the epoxidation product to obtain propylene oxide and propylene;
the epoxidation reaction unit comprises a first reaction zone, a second reaction zone and a third reaction zone, wherein the first reaction zone is arranged below the inner part of the reaction tank, is used for receiving the propylene to enter the reaction tank and is used as a main reaction site for propylene epoxidation reaction, and a first micro-interface generator connected with the propylene storage tank is arranged in the first reaction zone; the second reaction zone is arranged above the interior of the reaction tank, is connected with the mixed solvent storage tank, is used for receiving the mixed liquid, enters the interior of the reaction tank, and is used as a place for performing epoxidation on propylene which does not fully perform epoxidation in the first reaction zone and the third reaction zone, a separation layer is arranged inside the second reaction zone and is used for completely separating the second reaction zone from the third reaction zone, and a second micro-interface generator is arranged above the separation layer and is used for performing one-way communication between the second reaction zone and the third reaction zone; the third reaction zone with first reaction zone direct intercommunication, the third reaction zone set up in the retort middle part and be connected with vapour and liquid separator entry end for inside the epoxidation reaction product is carried to vapour and liquid separator, and as the epoxidation reaction place of the propylene that vapour and liquid separator separated out, inside is provided with the third micro interface generator who links to each other with the vapour and liquid separator exit end, the retort outside is provided with the circulating pump, the circulating pump entrance point is connected with the second reaction zone, the exit end is connected with third micro interface generator, be used for carrying the mixed liquid that the second reaction zone received to third reaction zone and first reaction zone.
Further, in the etherification-free system for preparing propylene oxide by enhanced propylene epoxidation, the first micro-interface generator adopts a pneumatic micro-interface generator, and is used for crushing propylene gas into micron-sized bubbles before the propylene in the first reaction zone undergoes epoxidation reaction, so that the contact area between the propylene and hydrogen peroxide in the mixed solution is increased, and the epoxidation reaction of the propylene is more sufficient.
Further, in the etherification-free system for preparing propylene oxide by the enhanced epoxidation of propylene, the second micro-interface generator is a pneumatic micro-interface generator, and is used as a channel for allowing propylene which is not subjected to epoxidation reaction in the first reaction zone and the third reaction zone to enter the second reaction zone, and the propylene which is not subjected to epoxidation reaction is crushed into micron-sized bubbles.
Further, in the etherification-free system for preparing propylene oxide by the enhanced epoxidation of propylene, the third micro-interface generator adopts a hydraulic micro-interface generator, and is used for absorbing propylene separated by the gas-liquid separator into the third micro-interface generator, crushing the absorbed propylene into micron-sized bubbles, and then releasing the micron-sized bubbles to the third reaction zone.
Furthermore, in the etherification-free system for preparing propylene oxide by the epoxidation of reinforced propylene, a buffer grid plate is arranged above the third micro-interface generator of the third reaction zone and is used for preventing the solution in the reaction tank from being vigorously boiled.
An etherification-free process for preparing propylene oxide by the epoxidation of reinforced propylene, which is characterized by comprising the following steps:
adding sufficient propylene into a propylene storage tank, and simultaneously adding hydrogen peroxide, acetonitrile and a catalyst into a mixed solvent storage tank according to corresponding proportions to prepare a uniformly mixed solution for later use;
and conveying the propylene to the first micro-interface generator, releasing the propylene to the first reaction zone, gradually introducing the propylene into the third reaction zone, and introducing the propylene into the second reaction zone through the second micro-interface generator on the separation layer until the interior of the reaction tank is filled with the propylene. Then conveying the mixed solution to a second reaction zone in the reaction tank, wherein the mixed solution cannot flow into a third reaction zone from a second micro-interface generator under the action of air pressure because the reaction tank is filled with propylene, and can only enter the third micro-interface generator through a circulating pump and then be released to the third reaction zone and the first reaction zone;
the first micro-interface generator breaks the propylene into micron-sized bubbles, the micron-sized bubbles are released to a first reaction zone, and when the mixed solution flows into the first reaction zone, the propylene micron-sized bubbles and hydrogen peroxide in the mixed solution are subjected to epoxidation reaction;
the propylene which is not fully reacted in the first reaction zone enters the second micro-interface generator through the separation layer, the second micro-interface generator breaks the propylene which is not fully reacted into micron-sized bubbles, the micron-sized bubbles are released to the second reaction zone to be subjected to epoxidation reaction with the hydrogen peroxide in the mixed solution, and an epoxidation reaction product and the mixed solution are conveyed to the inside of the third micro-interface generator through the circulating pump and then released to the third reaction zone;
and conveying the epoxidation reaction product into a gas-liquid separator for gas-liquid separation, conveying the separated propylene gas into a third micro-interface generator, crushing the separated propylene gas into micron-sized bubbles by the third micro-interface generator, releasing the micron-sized bubbles into a third reaction zone for epoxidation reaction with hydrogen peroxide in the mixed solution, and collecting the separated propylene oxide through an outlet below the separator.
Further, in the non-etherification process for preparing propylene oxide by the enhanced epoxidation of propylene, the micro-interface generator converts the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of gas and transmits the surface energy to the propylene gas, so that the propylene gas is broken into micron-sized bubbles with the diameter of micron level.
Furthermore, in the etherification-free process for preparing the propylene oxide by the enhanced propylene epoxidation, the micron-sized bubbles are micron-sized bubbles with the diameter of more than or equal to 1 μm and less than 1 mm.
Furthermore, in the etherification-free process for preparing the propylene oxide by the epoxidation of the reinforced propylene, the reaction pressure of the epoxidation reaction is 0.12-0.2 MPa.
Furthermore, in the etherification-free process for preparing the propylene oxide by the epoxidation of the reinforced propylene, the reaction temperature of the epoxidation reaction is 50-58 ℃.
In summary, the etherification-free system and process for preparing propylene oxide by the enhanced epoxidation of propylene provided by the invention have the beneficial effects that acetonitrile is selected as a solvent, the epoxidation activity is lower than that of an alcohol solvent due to the fact that acetonitrile is used as an aprotic solvent, the acetonitrile has inert and weak alkaline properties to effectively inhibit the ring opening of propylene oxide, so that etherification and hydrolysis byproducts are avoided, and a large amount of salt-containing wastewater and organic chloride are not contained in a product, so that equipment is not seriously corroded, and the system is provided with a micro-interface generator, so that propylene gas is crushed into micron-sized bubbles with the diameter of more than or equal to 1 μm and less than 1mm by the micro-interface generator before the epoxidation of propylene occurs, so that the contact area between propylene and hydrogen peroxide in the mixed solution is increased, and the epoxidation of propylene is more sufficient, the method achieves the effects of no equipment corrosion and no generation of ether products in the process of preparing the propylene oxide. In addition, the range of the preset operation condition can be flexibly adjusted according to different working conditions, different product requirements or different catalysts, so that the full and effective reaction is further ensured, the reaction rate is further ensured, and the purpose of strengthening the reaction is achieved.
Particularly, the system is provided with a first reaction zone, a second reaction zone and a third reaction zone which are respectively used for receiving propylene, allowing the propylene to enter the reaction tank, serving as a main reaction site for propylene epoxidation, receiving the mixed liquid, allowing the mixed liquid to enter the reaction tank, serving as propylene which is not subjected to the epoxidation in the first reaction zone, performing epoxidation, conveying products of the epoxidation to the inside of the gas-liquid separator, and serving as an epoxidation site for the propylene separated by the gas-liquid separator, so that the propylene can be fully utilized in the system, and the production cost is reduced.
Particularly, the buffering grid plate is arranged above the second micro-interface generator of the second reaction zone in the system, and when the temperature in the system is too high or the reaction is too severe, the buffering grid plate effectively avoids the damage to the reaction tank caused by the severe boiling in the reaction tank, so that the service life of the reaction tank is prolonged.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
fig. 1 is a schematic structural diagram of an etherification-free system and process for preparing propylene oxide by the enhanced epoxidation of propylene according to an embodiment of the present invention.
Detailed Description
In order that the objects and advantages of the invention will be more clearly understood, the invention is further described below with reference to examples; it should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
It should be noted that in the description of the present invention, the terms of direction or positional relationship indicated by the terms "upper", "lower", "left", "right", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, which are only for convenience of description, and do not indicate or imply that the device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
Furthermore, it should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Referring to fig. 1, the non-etherification system for preparing propylene oxide by enhanced propylene epoxidation provided by the embodiment of the present invention includes a reaction tank 3 having a first reaction area, a second reaction area and a third reaction area inside, the first reaction area is connected to a propylene storage tank 1 for storing and transporting propylene, the second reaction area is connected to a mixed solvent storage tank 2 for preparing and transporting a mixed solution of hydrogen peroxide, acetonitrile and a catalyst, the third reaction area is connected to a gas-liquid separator 4 for receiving propylene epoxidation products and performing gas-liquid separation on the epoxidation products, and a circulation pump 36 communicating the second reaction area and the third reaction area is disposed outside the reaction tank 3.
Before the system is started, sufficient propylene is added into the propylene storage tank, and simultaneously hydrogen peroxide, acetonitrile and a catalyst are added into the mixed solvent storage tank 2 according to corresponding proportions to prepare a uniformly mixed solution.
With continued reference to fig. 1, a first reaction zone is disposed below the interior of the reaction tank 3, and a first micro-interface generator 31 is disposed in the first reaction zone. The first micro-interface generator 31 is fixedly connected with the inside of the reaction tank 3, and the inlet end of the first micro-interface generator is connected with the propylene storage tank 1. Starting the system, delivering the propylene to the first micro-interface generator 31, releasing the propylene to the first reaction zone, gradually introducing the propylene to the third reaction zone, and then introducing the propylene to the second reaction zone through the second micro-interface generator 32 on the separation layer 34 until the inside of the reaction tank 3 is filled with the propylene. Then the mixed solution is transported to the second reaction area inside the reaction tank 3, and because the inside of the reaction tank 3 is filled with propylene, the mixed solution will not flow into the third reaction area from the second micro-interface generator 32 under the action of air pressure, and can only enter the third micro-interface generator 33 through the circulating pump 36, and then is released to the third reaction area and the first reaction area. The first micro-interface generator 31 breaks the propylene into micro-bubbles with a diameter of 1 μm or more and less than 1mm, and releases the micro-bubbles to the first reaction zone, and when the mixed solution flows into the first reaction zone, the micro-bubbles of propylene and the hydrogen peroxide in the mixed solution undergo an epoxidation reaction.
Continuing to refer to fig. 1, a second reaction zone connected to the mixed solvent storage tank 2 is disposed above the interior of the reaction tank 3, a separation layer 34 is fixedly connected to the second reaction zone for separating the second reaction zone from the substances in the first reaction zone and the third reaction zone, a second micro-interface generator 32 is disposed above the separation layer 34, and an inlet end of the second micro-interface generator is communicated with the first reaction zone and the third reaction zone. The propylene which is not fully reacted in the first reaction zone and the generated waste gas enter the second micro-interface generator 32 through the separation layer 34, the second micro-interface generator 32 breaks the propylene which is not fully reacted into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm, the micron-sized bubbles are released to the second reaction zone to generate epoxidation reaction with the hydrogen peroxide in the mixed solution, the products of the epoxidation reaction and the mixed solution are conveyed to the third reaction zone through the circulating pump 36, and the waste gas is discharged out of the reaction tank 3.
The middle part of the reaction tank 3 is provided with a third reaction zone connected with the inlet end of the gas-liquid separator 4, the third reaction zone is internally and fixedly connected with a third micro-interface generator 33, the third micro-interface generator 33 is respectively connected with the outlet end of the gas-liquid separator 4 and the outlet end of the circulating pump 36, and a heat exchanger 37 is arranged between the third micro-interface generator 33 and the circulating pump 36. A buffer grid 35 is provided above the third micro-interface generator 33 to prevent the solution inside the reaction tank 3 from boiling vigorously. Epoxidation reaction products in the first reaction zone and the second reaction zone are conveyed into a gas-liquid separator 4 for gas-liquid separation, separated propylene gas is conveyed into a third interface generator, the third micro-interface generator 33 breaks the separated propylene gas into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm, the micron-sized bubbles are released into the third reaction zone to perform epoxidation reaction with hydrogen peroxide in the mixed solution, separated propylene oxide finished products are collected through an outlet at the lower part of the separator, and waste liquid generated in a reaction tank 3 of the reaction tank 3 is discharged through a waste liquid channel.
Preferably, the micro-interface generator converts pressure energy of gas and/or kinetic energy of liquid into liquid surface energy and transmits the liquid surface energy to liquid chlorine, so that the liquid chlorine is broken into micron-sized bubbles with the diameter of micron level, and the micron-sized bubbles are divided into a pneumatic micro-interface generator, a hydraulic micro-interface generator and an air-liquid linkage micro-interface generator according to an energy input mode or a gas-liquid ratio, wherein the pneumatic micro-interface generator is driven by gas, and the input gas amount is far larger than the liquid amount; the hydraulic micro-interface generator is driven by liquid, and the input air quantity is generally smaller than the liquid quantity; the gas-liquid linkage type micro-interface generator is driven by gas and liquid at the same time, and the input gas amount is close to the liquid amount. The first micro-interface generator 31 and the second micro-interface generator 32 are pneumatic micro-interface generators, and the third micro-interface generator 33 is a hydraulic micro-interface generator.
The etherification-free system for preparing the propylene oxide by the epoxidation of the reinforced propylene selects the acetonitrile as a solvent, because acetonitrile is used as an aprotic solvent, the epoxidation reaction activity is lower than that of the epoxidation reaction using an alcohol solvent, the acetonitrile has the inertia and weak base performance to effectively inhibit the ring opening of the propylene oxide, thereby avoiding generating etherification and hydrolysis byproducts, and the products do not contain a large amount of salt-containing wastewater and organic chloride, thereby not causing serious corrosion of equipment, and the system is provided with the micro-interface generator which can break the propylene gas into micron-sized bubbles with the diameter more than or equal to 1 mu m and less than 1mm before the propylene generates epoxidation reaction, thereby increasing the contact area of the propylene and the hydrogen peroxide in the mixed solution, leading the epoxidation reaction of the propylene to be more sufficient, and achieving the effects of not causing equipment corrosion and not generating ether products in the process of preparing the propylene oxide.
The specific method and effect of the system of the present invention will be further described with reference to fig. 1.
An etherification-free process for preparing propylene oxide by the epoxidation of reinforced propylene, which comprises the following steps:
adding sufficient propylene into a propylene storage tank, and simultaneously adding hydrogen peroxide, acetonitrile and a catalyst into a mixed solvent storage tank according to corresponding proportions to prepare a uniformly mixed solution for later use;
conveying the propylene to a first micro-interface generator, releasing the propylene to a first reaction zone, gradually conveying the propylene to a third reaction zone, then conveying the propylene to a second reaction zone through a second micro-interface generator on a separation layer until the interior of a reaction tank is filled with the propylene, and then conveying the mixed solution to the second reaction zone in the reaction tank;
the first micro-interface generator breaks the propylene into micron-sized bubbles, the micron-sized bubbles are released to a first reaction zone, and when the mixed solution flows into the first reaction zone, the propylene micron-sized bubbles and hydrogen peroxide in the mixed solution are subjected to epoxidation reaction;
the propylene which is not fully reacted in the first reaction zone enters the second micro-interface generator through the separation layer, the second micro-interface generator breaks the propylene which is not fully reacted into micron-sized bubbles, the micron-sized bubbles are released to the second reaction zone to be subjected to epoxidation reaction with the hydrogen peroxide in the mixed solution, and an epoxidation reaction product and the mixed solution are conveyed to the inside of the third micro-interface generator through the circulating pump and then released to the third reaction zone;
and conveying the epoxidation reaction product into a gas-liquid separator for gas-liquid separation, conveying the separated propylene gas into a third micro-interface generator, crushing the separated propylene gas into micron-sized bubbles by the third micro-interface generator, releasing the micron-sized bubbles into a third reaction zone for epoxidation reaction with hydrogen peroxide in the mixed solution, and collecting the separated propylene oxide through an outlet below the separator.
Preferably, the reaction pressure of the epoxidation reaction is 0.1 to 0.2 MPa.
Preferably, the reaction temperature for the epoxidation reaction is 50 to 58 ℃.
In order to further verify the processing method provided by the invention, the beneficial effects of the invention are further illustrated by combining the examples. Meanwhile, in the present embodiment, the kind of the catalyst is not particularly limited, and may be one or a combination of several of an iron-based catalyst, a molybdenum-based catalyst, a nickel-based catalyst, a cobalt-based catalyst, and a tungsten-based catalyst, as long as the strengthening reaction can be smoothly performed.
Example 1:
adding sufficient propylene into a propylene storage tank, simultaneously adding hydrogen peroxide and acetonitrile into a mixed solvent storage tank to prepare a uniformly mixed solution, wherein the mass fraction of the hydrogen peroxide in the mixed solution is 40%, adding a proper amount of TS-1 catalyst into the mixed solvent storage tank, and controlling the temperature in a reaction tank at 50 ℃ and the pressure at 0.1 MPa;
conveying the propylene to a first micro-interface generator, releasing the propylene to a first reaction zone, gradually conveying the propylene to a third reaction zone, then conveying the propylene to a second reaction zone through a second micro-interface generator on a separation layer until the inside of a reaction tank is filled with the propylene, then slowly conveying 500g of mixed solution to the second reaction zone inside the reaction tank, conveying the mixed solution to the third micro-interface generator through a circulating pump, and releasing the propylene to the third reaction zone and the first reaction zone;
the first micro-interface generator breaks the propylene into micron-sized bubbles, the micron-sized bubbles are released to a first reaction zone, and when the mixed solution flows into the first reaction zone, the propylene micron-sized bubbles and hydrogen peroxide in the mixed solution are subjected to epoxidation reaction;
the propylene which is not fully reacted in the first reaction zone enters the second micro-interface generator through the separation layer, the second micro-interface generator breaks the propylene which is not fully reacted into micron-sized bubbles, the micron-sized bubbles are released to the second reaction zone to be subjected to epoxidation reaction with the hydrogen peroxide in the mixed solution, and an epoxidation reaction product and the mixed solution are conveyed to the inside of the third micro-interface generator through the circulating pump and then released to the third reaction zone;
conveying the epoxidation reaction product into a gas-liquid separator for gas-liquid separation, conveying the separated propylene gas into a third interface generator, crushing the separated propylene gas into micron-sized bubbles by the third micro-interface generator, releasing the micron-sized bubbles into a third reaction zone for epoxidation reaction with hydrogen peroxide in the mixed solution, and collecting the separated propylene oxide through an outlet below the separator;
after the reaction was completed, the conversion of hydrogen peroxide was measured to be 93%, the selectivity of propylene oxide was measured to be 85%, the ether product content was measured to be 0%, and the organic chloride content was measured to be 0%.
Example 2:
adding sufficient propylene into a propylene storage tank, simultaneously adding hydrogen peroxide and acetonitrile into a mixed solvent storage tank to prepare a uniformly mixed solution, wherein the mass fraction of the hydrogen peroxide in the mixed solution is 40%, adding a proper amount of TS-1 catalyst into the mixed solvent storage tank, and controlling the temperature in a reaction tank at 54 ℃ and the pressure at 0.15 MPa;
conveying the propylene to a first micro-interface generator, releasing the propylene to a first reaction zone, gradually conveying the propylene to a third reaction zone, then conveying the propylene to a second reaction zone through a second micro-interface generator on a separation layer until the inside of a reaction tank is filled with the propylene, then slowly conveying 1000g of mixed solution to the second reaction zone inside the reaction tank, conveying the propylene to the third micro-interface generator through a circulating pump, and releasing the propylene to the third reaction zone and the first reaction zone;
the first micro-interface generator breaks the propylene into micron-sized bubbles, the micron-sized bubbles are released to a first reaction zone, and when the mixed solution flows into the first reaction zone, the propylene micron-sized bubbles and hydrogen peroxide in the mixed solution are subjected to epoxidation reaction;
the propylene which is not fully reacted in the first reaction zone enters the second micro-interface generator through the separation layer, the second micro-interface generator breaks the propylene which is not fully reacted into micron-sized bubbles, the micron-sized bubbles are released to the second reaction zone to be subjected to epoxidation reaction with the hydrogen peroxide in the mixed solution, and an epoxidation reaction product and the mixed solution are conveyed to the inside of the third micro-interface generator through the circulating pump and then released to the third reaction zone;
conveying the epoxidation reaction product into a gas-liquid separator for gas-liquid separation, conveying the separated propylene gas into a third interface generator, crushing the separated propylene gas into micron-sized bubbles by the third micro-interface generator, releasing the micron-sized bubbles into a third reaction zone for epoxidation reaction with hydrogen peroxide in the mixed solution, and collecting the separated propylene oxide through an outlet below the separator;
after the reaction was completed, the conversion of hydrogen peroxide was found to be 95%, the selectivity of propylene oxide was found to be 89%, the ether product content was found to be 0%, and the organic chloride content was found to be 0%.
Example 3:
adding sufficient propylene into a propylene storage tank, simultaneously adding hydrogen peroxide and acetonitrile into a mixed solvent storage tank to prepare a uniformly mixed solution, wherein the mass fraction of the hydrogen peroxide in the mixed solution is 40%, adding a proper amount of TS-1 catalyst into the mixed solvent storage tank, and controlling the temperature in a reaction tank at 58 ℃ and the pressure at 0.2 MPa;
conveying the propylene to a first micro-interface generator, releasing the propylene to a first reaction zone, gradually conveying the propylene to a third reaction zone, then conveying the propylene to a second reaction zone through a second micro-interface generator on a separation layer until the inside of a reaction tank is filled with the propylene, then slowly conveying 1000g of mixed solution to the second reaction zone inside the reaction tank, conveying the propylene to the third micro-interface generator through a circulating pump, and releasing the propylene to the third reaction zone and the first reaction zone;
the first micro-interface generator breaks the propylene into micron-sized bubbles, the micron-sized bubbles are released to a first reaction zone, and when the mixed solution flows into the first reaction zone, the propylene micron-sized bubbles and hydrogen peroxide in the mixed solution are subjected to epoxidation reaction;
the propylene which is not fully reacted in the first reaction zone enters the second micro-interface generator through the separation layer, the second micro-interface generator breaks the propylene which is not fully reacted into micron-sized bubbles, the micron-sized bubbles are released to the second reaction zone to be subjected to epoxidation reaction with the hydrogen peroxide in the mixed solution, and an epoxidation reaction product and the mixed solution are conveyed to the inside of the third micro-interface generator through the circulating pump and then released to the third reaction zone;
conveying the epoxidation reaction product into a gas-liquid separator for gas-liquid separation, conveying the separated propylene gas into a third interface generator, crushing the separated propylene gas into micron-sized bubbles by the third micro-interface generator, releasing the micron-sized bubbles into a third reaction zone for epoxidation reaction with hydrogen peroxide in the mixed solution, and collecting the separated propylene oxide through an outlet below the separator;
after the reaction was completed, the conversion of hydrogen peroxide was 97%, the selectivity of propylene oxide was 92%, the ether product content was 0%, and the organic chloride content was 0% were measured.
In view of the above, the invention provides an etherification-free process for preparing propylene oxide by the enhanced epoxidation of propylene, which achieves the effects of no equipment corrosion and no generation of ether products in the preparation process of propylene oxide.
The above-mentioned embodiments are merely illustrative and not restrictive, and those skilled in the art can modify the embodiments without inventive contribution as required after reading this specification, but only fall within the scope of the claims of the present invention.
Claims (10)
1. An etherification-free system for producing propylene oxide by the epoxidation of propylene, comprising:
a propylene storage tank for storing and transporting propylene;
the mixed solvent storage tank is used for preparing and conveying mixed liquid of hydrogen peroxide, acetonitrile and a catalyst;
the gas-liquid separator is used for receiving the propylene epoxidation product and carrying out gas-liquid separation on the epoxidation product to obtain propylene oxide and propylene;
the epoxidation reaction unit comprises a first reaction zone, a second reaction zone and a third reaction zone, wherein the first reaction zone is arranged below the inner part of the reaction tank, is used for receiving the propylene to enter the reaction tank and is used as a main reaction site for propylene epoxidation reaction, and a first micro-interface generator connected with the propylene storage tank is arranged in the first reaction zone; the second reaction zone is arranged above the interior of the reaction tank, is connected with the mixed solvent storage tank, is used for receiving the mixed liquid, enters the interior of the reaction tank, and is used as a place for performing epoxidation on propylene which does not fully perform epoxidation in the first reaction zone and the third reaction zone, a separation layer is arranged inside the second reaction zone and is used for completely separating the second reaction zone from the third reaction zone, and a second micro-interface generator is arranged above the separation layer and is used for performing one-way communication between the second reaction zone and the third reaction zone; the third reaction zone with first reaction zone direct intercommunication, the third reaction zone set up in the retort middle part and be connected with vapour and liquid separator entry end for inside the epoxidation reaction product is carried to vapour and liquid separator, and as the epoxidation reaction place of the propylene that vapour and liquid separator separated out, inside is provided with the third micro interface generator who links to each other with the vapour and liquid separator exit end, the retort outside is provided with the circulating pump, the circulating pump entrance point is connected with the second reaction zone, the exit end is connected with third micro interface generator, be used for carrying the mixed liquid that the second reaction zone received to third reaction zone and first reaction zone.
2. The etherification-free system for preparing propylene oxide through intensified propylene epoxidation according to claim 1, wherein the first micro-interface generator is a pneumatic micro-interface generator, and is used for breaking propylene gas into micron-sized bubbles before the propylene in the first reaction zone undergoes epoxidation, so as to increase the contact area between propylene and hydrogen peroxide in the mixed solution, and make the epoxidation of propylene more complete.
3. The etherification-free system for preparing propylene oxide through the epoxidation of propylene in accordance with claim 1, wherein the second micro-interface generator is a pneumatic micro-interface generator for serving as a channel for the propylene which is not subjected to the epoxidation reaction in the first reaction zone and the third reaction zone to enter the second reaction zone and breaking the propylene which is not subjected to the epoxidation reaction into micron-sized bubbles.
4. The etherification system for preparing propylene oxide through the epoxidation of enhanced propylene according to claim 1, wherein the third micro-interface generator is a hydraulic micro-interface generator, and is used for entraining propylene separated by the gas-liquid separator into the third micro-interface generator, breaking the entrained propylene into micron-sized bubbles, and releasing the micron-sized bubbles into the third reaction zone.
5. The etherification-free system for producing propylene oxide through the epoxidation of propylene according to claim 1, wherein a buffer grid is disposed above the third micro-interface generator in the third reaction zone for preventing the solution in the reaction tank from boiling vigorously.
6. An etherification-free process for preparing propylene oxide by the epoxidation of reinforced propylene, which is characterized by comprising the following steps:
adding sufficient propylene into a propylene storage tank, and simultaneously adding hydrogen peroxide, acetonitrile and a catalyst into a mixed solvent storage tank according to corresponding proportions to prepare a uniformly mixed solution for later use;
conveying the propylene to a first micro-interface generator, releasing the propylene to a first reaction zone, gradually conveying the propylene to a third reaction zone, then conveying the propylene to a second reaction zone through a second micro-interface generator on a separation layer until the interior of a reaction tank is filled with the propylene, and then conveying the mixed solution to the second reaction zone in the reaction tank;
the first micro-interface generator breaks the propylene into micron-sized bubbles, the micron-sized bubbles are released to a first reaction zone, and when the mixed solution flows into the first reaction zone, the propylene micron-sized bubbles and hydrogen peroxide in the mixed solution are subjected to epoxidation reaction;
the propylene which is not fully reacted in the first reaction zone enters the second micro-interface generator through the separation layer, the second micro-interface generator breaks the propylene which is not fully reacted into micron-sized bubbles, the micron-sized bubbles are released to the second reaction zone to be subjected to epoxidation reaction with the hydrogen peroxide in the mixed solution, and an epoxidation reaction product and the mixed solution are conveyed to the inside of the third micro-interface generator through the circulating pump and then released to the third reaction zone;
and conveying the epoxidation reaction product into a gas-liquid separator for gas-liquid separation, conveying the separated propylene gas into a third micro-interface generator, crushing the separated propylene gas into micron-sized bubbles by the third micro-interface generator, releasing the micron-sized bubbles into a third reaction zone for epoxidation reaction with hydrogen peroxide in the mixed solution, and collecting the separated propylene oxide through an outlet below the separator.
7. The etherification-free process for preparing propylene oxide through the epoxidation of propylene according to claim 6, wherein the micro-interface generator converts the pressure energy of the gas and/or the kinetic energy of the liquid into the surface energy of the gas and transmits the surface energy to the propylene gas, so that the propylene gas is broken into micron-sized bubbles with the diameter of micron scale.
8. The etherification-free process for preparing propylene oxide through the epoxidation of propylene according to claims 1 to 7, wherein the micron-sized bubbles are micron-sized bubbles with the diameter of 1 μm or more and less than 1 mm.
9. The etherification-free process for preparing propylene oxide through the epoxidation of reinforced propylene according to claim 6, wherein the reaction pressure of the epoxidation reaction is 0.1-0.2 MPa.
10. The etherification-free process for preparing propylene oxide through the epoxidation of propylene according to claim 6, wherein the reaction temperature of the epoxidation reaction is 50-58 ℃.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910867736.1A CN112500371B (en) | 2019-09-14 | 2019-09-14 | Etherification-free system and process for preparing propylene oxide by virtue of intensified propylene epoxidation |
| PCT/CN2019/120194 WO2021047055A1 (en) | 2019-09-14 | 2019-11-22 | Etherification-free system and process for preparing epoxypropane by strengthening propylene epoxidation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910867736.1A CN112500371B (en) | 2019-09-14 | 2019-09-14 | Etherification-free system and process for preparing propylene oxide by virtue of intensified propylene epoxidation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112500371A true CN112500371A (en) | 2021-03-16 |
| CN112500371B CN112500371B (en) | 2023-04-11 |
Family
ID=74866906
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910867736.1A Active CN112500371B (en) | 2019-09-14 | 2019-09-14 | Etherification-free system and process for preparing propylene oxide by virtue of intensified propylene epoxidation |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN112500371B (en) |
| WO (1) | WO2021047055A1 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102532063A (en) * | 2011-11-17 | 2012-07-04 | 大连理工大学 | Device and method for performing olefin gaseous phase epoxidation by using industrial hydrogen peroxide |
| CN104557779A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Production method of epoxy propane |
| CN105272944A (en) * | 2014-07-24 | 2016-01-27 | 中国石油化工股份有限公司 | Method for preparing epoxy propane through epoxidation of ethylbenzene hydroperoxide and propylene |
| CN105272938A (en) * | 2014-07-24 | 2016-01-27 | 中国石油化工股份有限公司 | Epoxidation cyclic method for preparing epoxy propane from ethylbenzene hydroperoxide and propylene |
| CN105294606A (en) * | 2014-07-24 | 2016-02-03 | 中国石油化工股份有限公司 | Reaction method for preparation propylene oxide from hydrogen peroxide ethylbenzene and propene |
| CN105315235A (en) * | 2014-07-24 | 2016-02-10 | 中国石油化工股份有限公司 | Method used for realizing epoxidation of hydrogen peroxide ethylbenzene with propylene |
| CN105330618A (en) * | 2015-11-24 | 2016-02-17 | 扬州大学 | Method for producing propylene epoxide by trickle bed reactor |
| CN109912542A (en) * | 2019-03-28 | 2019-06-21 | 江苏扬农化工集团有限公司 | A kind of method that the homogeneous system of low propylene usage amount prepares propylene oxide |
| CN211487597U (en) * | 2019-09-14 | 2020-09-15 | 南京延长反应技术研究院有限公司 | Etherification-free system for preparing propylene oxide by epoxidation of reinforced propylene |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2810980B1 (en) * | 2000-06-28 | 2004-05-21 | Solvay | PROCESS FOR THE MANUFACTURE OF OXIRANNE IN THE PRESENCE OF A CATALYST IN THE FORM OF PARTICLES |
| DE10320635A1 (en) * | 2003-05-08 | 2004-11-18 | Basf Ag | Process for the production of propylene oxide |
| WO2010077823A2 (en) * | 2008-12-16 | 2010-07-08 | H R D Corporation | High shear oxidation of wax |
| CN108191794B (en) * | 2017-12-29 | 2020-02-11 | 中触媒新材料股份有限公司 | Propylene epoxidation reaction method |
-
2019
- 2019-09-14 CN CN201910867736.1A patent/CN112500371B/en active Active
- 2019-11-22 WO PCT/CN2019/120194 patent/WO2021047055A1/en active Application Filing
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102532063A (en) * | 2011-11-17 | 2012-07-04 | 大连理工大学 | Device and method for performing olefin gaseous phase epoxidation by using industrial hydrogen peroxide |
| CN104557779A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Production method of epoxy propane |
| CN105272944A (en) * | 2014-07-24 | 2016-01-27 | 中国石油化工股份有限公司 | Method for preparing epoxy propane through epoxidation of ethylbenzene hydroperoxide and propylene |
| CN105272938A (en) * | 2014-07-24 | 2016-01-27 | 中国石油化工股份有限公司 | Epoxidation cyclic method for preparing epoxy propane from ethylbenzene hydroperoxide and propylene |
| CN105294606A (en) * | 2014-07-24 | 2016-02-03 | 中国石油化工股份有限公司 | Reaction method for preparation propylene oxide from hydrogen peroxide ethylbenzene and propene |
| CN105315235A (en) * | 2014-07-24 | 2016-02-10 | 中国石油化工股份有限公司 | Method used for realizing epoxidation of hydrogen peroxide ethylbenzene with propylene |
| CN105330618A (en) * | 2015-11-24 | 2016-02-17 | 扬州大学 | Method for producing propylene epoxide by trickle bed reactor |
| CN109912542A (en) * | 2019-03-28 | 2019-06-21 | 江苏扬农化工集团有限公司 | A kind of method that the homogeneous system of low propylene usage amount prepares propylene oxide |
| CN211487597U (en) * | 2019-09-14 | 2020-09-15 | 南京延长反应技术研究院有限公司 | Etherification-free system for preparing propylene oxide by epoxidation of reinforced propylene |
Non-Patent Citations (1)
| Title |
|---|
| 张志炳;田洪舟;张锋;周政;: "多相反应体系的微界面强化简述" * |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2021047055A1 (en) | 2021-03-18 |
| CN112500371B (en) | 2023-04-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2022041426A1 (en) | Micro-interface preparation system and method for cyclic carbonate | |
| CN101384352A (en) | Micro channel device of unit operation after preparation of ethylene oxide | |
| WO2022041425A1 (en) | Reinforced micro-interface preparation system and method for cyclic carbonate | |
| GB2433500A (en) | Epoxidation of olefins by reacting olefin, oxygen & catalyst, & subsequent quenching & conversion of carbon dioxide, & chemicals derivable from olefin oxides | |
| CN112500371B (en) | Etherification-free system and process for preparing propylene oxide by virtue of intensified propylene epoxidation | |
| CN211487597U (en) | Etherification-free system for preparing propylene oxide by epoxidation of reinforced propylene | |
| WO2023138074A1 (en) | Method and system for preparing cyclic carbonate by catalyzing carbon dioxide cycloaddition | |
| CN107602510B (en) | Preparation method and production equipment of propylene oxide | |
| CN112044390A (en) | Preparation system and method of cyclic carbonate | |
| CN110813226A (en) | Chlorohydrination reaction device for chlorohydrination method epoxide production and use method thereof | |
| CN104774168B (en) | Method for coproduction of dicumyl peroxide (DCP) and epoxybutane (CHPBO) | |
| CN212120009U (en) | Etherification-free intelligent system for preparing propylene oxide by intensified propylene epoxidation | |
| CN112495312A (en) | Etherification-free intelligent system and process for preparing propylene oxide by intensified propylene epoxidation | |
| CN101687831A (en) | Method and apparatus for producing mixed gas, and apparatus and method for producing epoxy compound | |
| CN105498300B (en) | A kind of preparation method of ethylene oxide propylene oxide composite anti-foaming agent | |
| CN211814210U (en) | Micro-interface enhanced reaction system for preparing ethylene glycol based on ethylene hydration method | |
| CN109928943B (en) | Method for synthesizing propylene oxide by using microchannel reactor | |
| CN210674823U (en) | Wash oil and direct liquefied coal oil mixed processing system | |
| CN112028768A (en) | Reaction system and method for preparing glycolate through oxalate hydrogenation | |
| CN112479882A (en) | Reaction system and process for synthesizing dimethyl carbonate by liquid-phase oxidative carbonylation of methanol | |
| CN101103010B (en) | Method for producing propylene oxide | |
| CN215540716U (en) | Tower type enhanced oxidation system for preparing hydrogen peroxide | |
| CN109999728A (en) | A method of reducing the bed temperature rise of HPPO process catalyst | |
| CN108715575A (en) | Solid super base is the method that catalyst fixed bed reaction prepares dihydroxypropane single-ether | |
| CN108620055A (en) | It is used to prepare solid super basic catalyst and its application of dihydroxypropane single-ether |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |