CN114507116B - Olefin hydration reaction method - Google Patents
Olefin hydration reaction method Download PDFInfo
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- CN114507116B CN114507116B CN202011169944.3A CN202011169944A CN114507116B CN 114507116 B CN114507116 B CN 114507116B CN 202011169944 A CN202011169944 A CN 202011169944A CN 114507116 B CN114507116 B CN 114507116B
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- 150000001336 alkenes Chemical class 0.000 title claims abstract description 189
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims abstract description 175
- 238000006703 hydration reaction Methods 0.000 title claims abstract description 108
- 238000000034 method Methods 0.000 title claims abstract description 67
- 239000003054 catalyst Substances 0.000 claims abstract description 115
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 96
- 238000002156 mixing Methods 0.000 claims abstract description 81
- 230000036571 hydration Effects 0.000 claims abstract description 59
- 239000000463 material Substances 0.000 claims abstract description 55
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 239000000835 fiber Substances 0.000 claims description 63
- HGCIXCUEYOPUTN-UHFFFAOYSA-N cyclohexene Chemical compound C1CCC=CC1 HGCIXCUEYOPUTN-UHFFFAOYSA-N 0.000 claims description 50
- 239000010410 layer Substances 0.000 claims description 47
- 239000012071 phase Substances 0.000 claims description 34
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 claims description 25
- 238000009826 distribution Methods 0.000 claims description 18
- 230000003247 decreasing effect Effects 0.000 claims description 16
- 239000007788 liquid Substances 0.000 claims description 14
- -1 ethylene, propylene, n-butene Chemical class 0.000 claims description 13
- 239000006185 dispersion Substances 0.000 claims description 12
- 239000004743 Polypropylene Substances 0.000 claims description 11
- 229920001155 polypropylene Polymers 0.000 claims description 11
- 238000007599 discharging Methods 0.000 claims description 7
- 239000007795 chemical reaction product Substances 0.000 claims description 5
- 230000003068 static effect Effects 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- 229920000728 polyester Polymers 0.000 claims description 4
- BKOOMYPCSUNDGP-UHFFFAOYSA-N 2-methylbut-2-ene Chemical group CC=C(C)C BKOOMYPCSUNDGP-UHFFFAOYSA-N 0.000 claims description 3
- 125000003178 carboxy group Chemical group [H]OC(*)=O 0.000 claims description 3
- 239000002184 metal Substances 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 claims description 3
- 125000003368 amide group Chemical group 0.000 claims description 2
- 239000008346 aqueous phase Substances 0.000 claims description 2
- 239000000919 ceramic Substances 0.000 claims description 2
- 239000000084 colloidal system Substances 0.000 claims description 2
- 239000011521 glass Substances 0.000 claims description 2
- 125000002887 hydroxy group Chemical group [H]O* 0.000 claims description 2
- 239000012528 membrane Substances 0.000 claims description 2
- 229920001778 nylon Polymers 0.000 claims description 2
- 229920002239 polyacrylonitrile Polymers 0.000 claims description 2
- 229920000642 polymer Polymers 0.000 claims description 2
- 229920006306 polyurethane fiber Polymers 0.000 claims description 2
- 229920000915 polyvinyl chloride Polymers 0.000 claims description 2
- 239000004800 polyvinyl chloride Substances 0.000 claims description 2
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 claims description 2
- 239000011541 reaction mixture Substances 0.000 claims description 2
- 239000002356 single layer Substances 0.000 claims description 2
- 230000007423 decrease Effects 0.000 claims 2
- 238000006243 chemical reaction Methods 0.000 abstract description 79
- 239000002994 raw material Substances 0.000 abstract description 30
- 230000000694 effects Effects 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 239000012467 final product Substances 0.000 abstract 1
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 25
- BTANRVKWQNVYAZ-UHFFFAOYSA-N butan-2-ol Chemical compound CCC(C)O BTANRVKWQNVYAZ-UHFFFAOYSA-N 0.000 description 18
- 239000000203 mixture Substances 0.000 description 12
- 239000007858 starting material Substances 0.000 description 12
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 description 11
- 239000002245 particle Substances 0.000 description 8
- HPXRVTGHNJAIIH-UHFFFAOYSA-N cyclohexanol Chemical compound OC1CCCCC1 HPXRVTGHNJAIIH-UHFFFAOYSA-N 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 5
- 229910001220 stainless steel Inorganic materials 0.000 description 5
- 239000010935 stainless steel Substances 0.000 description 5
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 4
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 4
- 238000005728 strengthening Methods 0.000 description 4
- 238000006276 transfer reaction Methods 0.000 description 4
- MSXVEPNJUHWQHW-UHFFFAOYSA-N 2-methylbutan-2-ol Chemical compound CCC(C)(C)O MSXVEPNJUHWQHW-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005191 phase separation Methods 0.000 description 3
- 238000000066 reactive distillation Methods 0.000 description 3
- 229920005989 resin Polymers 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- 238000005520 cutting process Methods 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- YWAKXRMUMFPDSH-UHFFFAOYSA-N pentene Chemical compound CCCC=C YWAKXRMUMFPDSH-UHFFFAOYSA-N 0.000 description 2
- 239000003444 phase transfer catalyst Substances 0.000 description 2
- 239000011347 resin 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
- 229920002972 Acrylic fiber Polymers 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004952 Polyamide Substances 0.000 description 1
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 description 1
- 240000001949 Taraxacum officinale Species 0.000 description 1
- 235000005187 Taraxacum officinale ssp. officinale Nutrition 0.000 description 1
- KXKVLQRXCPHEJC-UHFFFAOYSA-N acetic acid trimethyl ester Natural products COC(C)=O KXKVLQRXCPHEJC-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- SRSXLGNVWSONIS-UHFFFAOYSA-N benzenesulfonic acid Chemical compound OS(=O)(=O)C1=CC=CC=C1 SRSXLGNVWSONIS-UHFFFAOYSA-N 0.000 description 1
- 229940092714 benzenesulfonic acid Drugs 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 229920001429 chelating resin Polymers 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000003495 polar organic solvent Substances 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- DCKVNWZUADLDEH-UHFFFAOYSA-N sec-butyl acetate Chemical compound CCC(C)OC(C)=O DCKVNWZUADLDEH-UHFFFAOYSA-N 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 238000005809 transesterification reaction Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/03—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2
- C07C29/04—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2 by hydration of carbon-to-carbon double bonds
Abstract
The invention discloses an olefin hydration reaction method, which comprises the following steps: a plurality of catalyst beds are arranged in the olefin hydration reactor, and the reaction mixed raw materials are divided into a feed I, a feed II and a feed III; feeding I enters a 1 st catalyst bed from the bottom of an olefin hydration reactor, feeding II is divided into x strands after mixing and dispersing, different beds are introduced between catalyst beds, feeding III is divided into y strands after mixing and dispersing, different beds are introduced between catalyst beds, and at least 1 strand of material in the x strands of feeding II and at least 1 strand of material in the y strands of feeding III are introduced into the same bed; the olefin hydration reaction of each feed takes place in the catalyst bed and the final product flows out through the top of the reactor. The method of the invention strengthens the main reaction effect by introducing two reaction raw materials with different proportions between catalyst beds, realizes the efficient mass transfer of olefin and water, greatly improves the hydration reaction rate of olefin and the single-pass conversion rate of raw materials, reduces the number and the volume of reactors and reduces the energy consumption in the separation process.
Description
Technical Field
The invention belongs to the technical field of organic chemical industry, and particularly relates to an olefin hydration reaction method.
Background
The olefin hydration process is a liquid (olefin) -liquid (water) -solid (catalyst) three-phase catalytic reaction, so the reaction rate and conversion rate are greatly affected by liquid-liquid mass transfer. The mutual solubility of the olefin and water is small, so that the reaction efficiency and the productivity of the olefin hydration process are limited. In the olefin hydration reaction, the typical and important olefin hydration reaction is to prepare cyclohexanol by cyclohexene hydration, sec-butanol by n-butene hydration and tert-butanol by isobutene hydration and tert-amyl alcohol by isoamylene hydration. The method is characterized in that the method is more typical in that cyclohexene is hydrated to prepare cyclohexyl alcohol and n-butene is hydrated to prepare sec-butyl alcohol, the single pass conversion rate in the prior art is low, the improvement of the production efficiency is restricted, a large amount of circulating materials are needed in the reaction, the reaction system is huge, and the energy consumption in the fractionation process is high.
In the process of preparing cyclohexanol by cyclohexene hydration, the reactor of the cyclohexene direct hydration production device currently used in industry is a two-stage series-connection full-mixing reactor, the single-pass conversion rate is only 9%, the selectivity is 99%, the single-pass conversion rate of cyclohexene hydration reaction is low, and a large amount of unreacted cyclohexene and cyclohexanol are separated by repeated circulating rectification, so that the energy consumption is high. Therefore, in order to increase the rate and conversion rate of cyclohexene hydration, CN 109651081A proposes a reactive distillation method and apparatus for preparing cyclohexanol by cyclohexene hydration, in which a phase transfer catalyst is added to a reaction solution to form a slurry solution of cyclohexene, water, catalyst and phase transfer catalyst, and cyclohexene hydration reaction occurs in a reactive distillation column to form cyclohexanol, and the reactive distillation method can greatly increase the conversion rate of cyclohexene and reduce the energy consumption of the system in theory, but has a slow hydration reaction rate. US3257469 uses polar organic solvents to increase the miscibility of olefins with water, thereby increasing the conversion of carbon penta-olefins by increasing the rate of diffusion of reactant molecules to the catalyst surface and the rate of diffusion of the product into the solvent. The U.S. patent No. 4182920 uses a three-stage olefin hydration reactor at a reaction temperature of 30-80 ℃ and a reaction pressure of 0.46-1.4 MPa (absolute pressure), the weight ratio of water to pentene is in the range of 0.59-1.18, the weight ratio of acetone to pentene is in the range of 4.18-7.85, and the reaction rate is still very slow.
In the process of preparing sec-butyl alcohol by hydration of n-butene, the mutual dissolution of hydrocarbons such as n-butene and water is poor, so that the phase separation of two liquid phases is easy to be caused during the liquid phase mixing and hydration reaction of two phases, and the mass transfer reaction rate of the two phases is low, and the single pass conversion rate is very low. CN20100000441.3 proposes a multifunctional group resin catalyst and its preparation method, especially suitable for preparing tert-butyl alcohol (TBA) by isobutene hydration, n-butyl alcohol (SBA) by n-butene hydration, isopropanol (IPA) by propylene hydration. The method mainly improves the hydration reaction rate of olefin from the aspect of improving the catalyst, and is not mentioned from the aspects of the process and the reactor. CN201210230912.9 proposes a method for synthesizing sec-butyl alcohol, which uses sec-butyl acetate and methanol as raw materials, produces sec-butyl alcohol through transesterification, and uses methyl acetate as a byproduct.
In summary, for the process of preparing cyclohexanol and sec-butyl alcohol by hydration of cyclohexene, the mass transfer reaction rate is greatly affected based on the problems of low intersolubility of olefin and water and easy phase separation, so that the two phases are in a highly mixed state and are not phase separated in the olefin hydration reaction process, which is a process route capable of effectively solving the problems of low reaction rate, long residence time and the like caused by low mass transfer rate of olefin hydration, and has important significance in greatly improving the olefin hydration reaction rate and single pass conversion rate.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides an olefin hydration reaction method, which strengthens the main reaction effect by introducing two reaction raw materials with different proportions between catalyst beds, realizes the efficient mass transfer of olefin and water, improves the olefin hydration reaction rate and the single-pass conversion rate of the raw materials under the condition of lower water-olefin ratio, reduces the number and the volume of reactors, and reduces the energy consumption in the separation process.
The olefin hydration reaction method of the invention comprises the following steps: a plurality of catalyst beds are arranged in the olefin hydration reactor, and the catalyst beds are the 1 st to the n th catalyst beds from bottom to top in sequence; dividing a reaction mixture comprising an olefin phase and an aqueous phase into a feed I, a feed II and a feed III; feeding I enters a 1 st catalyst bed layer from the bottom of an olefin hydration reactor, feeding II is divided into x strands after mixing and dispersing, different catalyst beds are introduced between the catalyst beds, feeding III is divided into y strands after mixing and dispersing, different catalyst beds are introduced between the catalyst beds, and at least 1 strand of material in the x strands of feeding II and at least 1 strand of material in the y strands of feeding III are introduced into the same catalyst bed; each feed is subjected to olefin hydration reaction in the catalyst bed, and the final reaction product flows out from the top of the reactor and enters the next separation unit; wherein the water-to-olefin ratio of the feed II is more than or equal to 1, preferably 1:1-10:1, and the water-to-olefin ratio of the feed III is less than 1, preferably 1:1.5-1:10; the x is less than n, y is less than n, n is more than or equal to 2, preferably n is less than or equal to 10, more preferably n is less than or equal to 5, and even more preferably x=y. The water-olefin ratio of the invention is the mass ratio of the water phase to the olefin phase.
In the method, the mass of olefin in the feed I accounts for 30% -98% of the total mass of olefin in the feed; the water-to-olefin ratio of the feed I is not particularly required, and is generally 1.0-20.0; the mass of the olefin in feed II is generally 1% to 35%, preferably 3% to 10% of the total feed olefin mass, and the mass of the olefin in feed III is generally 1% to 35%, preferably 5% to 20% of the total feed olefin mass; wherein the total feed olefin mass is the total mass of olefins in feed I, feed II and feed III.
In the method of the invention, the feed I is preferably mixed by a premixing device with a mixing function, such as one or more of static mixers, stirred tanks, colloid mills, inorganic membrane tube mixers and the like.
In the process of the present invention, the olefin feedstock is typically ethylene, propylene, n-butene, isobutylene, isoamylene, cyclohexene or the like.
In the method of the invention, the olefin hydration reactor is a fixed bed reactor, one or a plurality of olefin hydration reactors can be arranged, and the reactors can be connected in series or in parallel.
In the process of the invention, the mass ratio of feed II to feed III is from 1:50 to 50:1, preferably from 1:5 to 5:1; the material distribution is preferably carried out after the feed II and the feed III enter the reactor, the feed II and the feed III are uniformly distributed on the section of the reactor, the material distribution assembly is arranged in the reactor, and the structure of the distribution assembly can be any one of a pipe type, a branch type, a filling type and the like.
In the method of the invention, the total water-to-olefin ratio is determined according to the type of olefin and the difficulty of the reaction in which the olefin hydration reaction occurs, the total water-to-olefin mass ratio is generally 1:1-20:1, preferably 1:1-15:1, and a properly high water-to-olefin ratio can ensure the mass transfer reaction rate in the hydration process, but the reactor has larger volume and higher investment, and the determination of the water-to-olefin ratio is generally as low as possible on the premise of ensuring the single-pass conversion rate of the hydration reaction.
In the method of the invention, the mixing and dispersing of the feed II and the feed III are carried out by adopting any one of reinforced mixing equipment, such as jet mixing equipment, rotational flow mixing equipment, shearing mixing equipment, stirring mixing equipment, micro-channel mixing equipment and the like, and preferably adopting micro-channel mixing equipment.
The microchannel mixing device comprises a housing and at least one microchannel mixing assembly; the micro-channel component is fixed in the shell, one end of the shell is provided with an inlet for feeding the olefin phase and the water phase, and the other end of the shell is provided with an outlet for outflow of the mixed materials; the micro-channel assembly in the shell is divided into a feeding end and a discharging end along the crack direction, a feeding distribution space is arranged between the inlet of the shell and the feeding end, a discharging distribution space is arranged between the outlet of the shell and the discharging end, and in order to prevent short circuit of materials, the micro-channel assembly is ensured to flow from the feeding end to the discharging end in the micro-channel assembly, and all the other ends of the micro-channel assembly are in sealing connection with the shell except the feeding end and the discharging end. A plurality of serially connected micro-channel components can be arranged in the shell to improve the mixing effect.
The microchannel mixing assembly generally comprises a plurality of stacked sheets and lipophilic and/or hydrophilic filaments filled between the seams of adjacent sheets; the fiber filaments form a plurality of micro-channels, and are clamped and fixed by the thin sheet; the fiber filaments filled between the seams of the adjacent sheets can be arranged in a single layer or multiple layers, preferably 1-50 layers, more preferably 1-5 layers, and preferably the fiber filaments in any layer are uniformly distributed among the fiber filaments.
When the fiber filaments are arranged in multiple layers, the projection of two adjacent layers of fiber filaments along the vertical direction of the sheet is preferably a net structure; the mesh shape in the mesh structure can be any shape, such as one or more of a polygon, a circle, an ellipse, etc.; in each layer of fiber filaments, the spacing between adjacent fiber filaments is generally 0.5-50 μm, preferably the fiber filaments are distributed at equal intervals, and the fiber filaments are arranged along any one of the transverse direction, the longitudinal direction or the oblique direction of the surface of the sheet; the filaments may be of any curvilinear shape, preferably a periodically varying curvilinear shape, such as wavy, zigzag, etc., preferably the filaments of the same layer are of the same shape, more preferably the filaments of all layers are of the same shape.
The sheet thickness may be the same or different; the thickness of the sheet is generally 0.05mm to 5mm, preferably 0.1 to 1.5mm. The material of the sheet is generally determined by the nature of the overcurrent material and the operating conditions, and may be any of metal, ceramic, organic glass, polyester, etc., preferably stainless steel (SS 30403, SS 30508, SS32168, SS 31603) among metals. The shape of the sheet may be any of rectangle, square, polygon, circle, ellipse, fan, etc., preferably rectangle or square. The size and number of the flakes can be designed and adjusted according to the actual needs of the reaction.
Wherein the lipophilic fiber yarn is generally selected from at least one of polyester fiber yarn, nylon fiber yarn, polyurethane fiber yarn, polypropylene fiber yarn, polyacrylonitrile fiber yarn and polyvinyl chloride fiber yarn, or fiber yarn with surface subjected to lipophilic treatment by a physical or chemical method; the hydrophilic fiber yarn is generally selected from carboxyl (-COOH), amido (-CONH-) and amino (-NH) in main chain or side chain 2 Polymer containing hydrophilic groups such as (-) or hydroxyl (-OH), and having high hydrophilicity, such as polypropylene fiber, polyamide fiber, acrylic fiber, or other common polymerThe material is treated by physical or chemical hydrophilic method. Wherein, the types and the proportion of the fiber filaments filled between the cracks are adjusted according to the property of the dispersed material, and when the olefin phase is the dispersed phase, the proportion of the lipophilic fiber filaments and the hydrophilic fiber filaments filled between the micro-channel sheets is 50:1-1:1; when the water phase is a disperse phase, the ratio of the lipophilic fiber filaments to the hydrophilic fiber filaments filled among the micro-channel sheets is 1:1-1:50.
In the method of the invention, in the mixed and dispersed feed II, the dispersion size d1 of olefin liquid drops is 0.5-900 mu m, and in the mixed and dispersed feed III, the dispersion size d1 of water liquid drops is 0.5-900 mu m, preferably 100-500 mu m, and preferably the dispersion uniformity is more than or equal to 80%. At this time, when the two phases enter the catalyst bed layer of the reactor to react, the two phases of olefin/water can be kept not to be separated in the reaction residence time, and the mass transfer reaction rate is greatly improved under the condition of lower water-olefin ratio.
In the process of the invention, the mass of each of the x divided feed II strands in the material flow direction may be different or the same, preferably decreasing, in a proportion of generally 3 to 80%, preferably 10 to 50%, according to the reaction requirements.
In the method of the invention, in the y strands of the feed III, the mass of each stream in the material flow direction can be different or the same according to the reaction requirement, and the decreasing proportion is generally 3-80%, preferably 10-50%.
In the method of the invention, the catalyst bed layer adopts olefin hydration catalyst which is conventional in the art, such as mineral acid, benzenesulfonic acid, ion exchange resin, molecular sieve and other types of catalyst.
In the process of the present invention, the olefin hydration reaction conditions are generally: the temperature is 80-250 ℃, the pressure is 1.0-10.0 MPaG, and the airspeed is 0.1-3.0 h -1 The reaction conditions required for the olefin feed will vary.
In the prior art, the olefin/water mixing generally adopts a conventional method, mixing equipment or a component with a mixing function, the conventional material distribution is adopted during the reaction, and the problems of unsatisfactory mixing effect and easy phase separation in the reaction process exist, so that the mass transfer rate of olefin hydration is lower, the single pass conversion rate is low even at a higher water-olefin ratio, and particularly for normal butene hydration, the single pass conversion rate of a conventional reactor is only 6-8%. In the olefin hydration reactor and the olefin hydration method, an olefin/water mixture with a water-olefin ratio of more than or equal to 1 is introduced into micro-channel mixing equipment to form a feed II, and olefin is dispersed in water in a mode of micron-sized liquid drops; introducing an olefin/water mixture with the water-olefin ratio less than 1 into a microchannel mixing device to form a feed III, dispersing water in olefin in a micron-sized droplet manner, and introducing the feed II and the feed III between catalyst beds, so that a large number of evenly distributed micron-sized olefin droplets and micron-sized water droplets exist in the reaction material all the time, the intersolubility of olefin/water is enhanced, the efficient mass transfer of olefin and water is realized, the olefin hydration reaction rate and the single-pass conversion rate of raw materials are greatly improved under the condition of low water-olefin ratio, the water-olefin ratio is reduced, the number and the volume of the reactor are reduced, and the energy consumption in the separation process is reduced.
Drawings
FIG. 1 is a schematic diagram of an olefin hydration reactor of the present invention; FIG. 2 is a schematic diagram of a microchannel mixing device of the present invention.
Wherein 1 is an olefin raw material I,2 is water I,3 is a mixed feed I,4 is an olefin raw material II,5 is water II,6 is a micro-channel mixing device I,7 is a component of the micro-channel device I, 8 is a micro-channel sheet, 9 is a gap between micro-channel sheets, 10 is a hydrophilic/lipophilic fiber yarn, 11 is an olefin/water mixed feed II,12 is an olefin raw material, 13 is water, 14 is a micro-channel mixing device II,15 is a component of the micro-channel device II, 16 is a micro-channel sheet, 17 is a gap between micro-channel sheets, 18 is a hydrophilic/lipophilic fiber yarn, 19 is an olefin/water mixed feed III,20 is an olefin hydration reactor, 21 is an olefin/water mixed feed II entering the 1/2 catalyst bed layer, 22 is the olefin/water mixed feed II into the 2/3 rd catalyst bed, 23 is the olefin/water mixed feed II into the 3/4 th catalyst bed, 24 is the olefin/water mixed feed III into the 1/2 nd catalyst bed, 25 is the olefin/water mixed feed III into the 2/3 rd catalyst bed, 26 is the olefin/water mixed feed III into the 3/4 th catalyst bed, 27 is the 1 st catalyst bed, 28 is the 2 nd catalyst bed, 29 is the 3 rd catalyst bed, 30 is the 4 th catalyst bed, 31 is the 1/2 nd catalyst bed layer material distribution assembly, 32 is the 2/3 rd catalyst bed layer material distribution assembly, 33 is the 3/4 th catalyst bed layer material distribution assembly, 34 is the olefin hydration reaction product.
Detailed Description
The invention will now be described in more detail with reference to the accompanying drawings and examples, which are not intended to limit the invention thereto.
The olefin hydration reaction process of the present invention is illustrated in FIG. 1:
firstly, an olefin raw material I1 and water I2 are mixed and then are introduced into the bottom of an olefin hydration reactor 20 as a mixed feed I3, and an olefin hydration reaction gradually occurs from bottom to top in the reactor; mixing the other part of olefin raw material II 4 and water II 5 according to the ratio of water to olefin being more than or equal to 1, introducing the mixture into a gap 9 between micro-channel sheets 8 in a micro-channel assembly 7 arranged in micro-channel mixing equipment 6, continuously cutting hydrophilic/lipophilic fiber filaments 10 filled between the gap 9 for a plurality of times to form olefin/water mixed feed II 11, wherein the olefin/water mixed feed II 21 serving as a 1/2 catalyst bed layer, the olefin/water mixed feed II 22 of a 2/3 catalyst bed layer and the olefin/water mixed feed II 23 of a 3/4 catalyst bed layer are respectively introduced into the 1/2, 2/3 and 3/4 catalyst bed layers; after mixing the other part of olefin raw material 12 and water 13 in the ratio of water to olefin ratio less than 1, the olefin/water mixed feed III 19 is formed after passing through the gaps 17 among the micro-channel thin sheets 16 in the micro-channel assembly 15 arranged in the micro-channel mixing equipment 14 and continuously cutting the hydrophilic/lipophilic fiber filaments 18 filled among the gaps 17 for a plurality of times, and the olefin/water mixed feed III 24 serving as the 1 st/2 nd catalyst bed layer, the olefin/water mixed feed III 25 of the 2 nd/3 rd catalyst bed layer and the olefin/water mixed feed III 26 of the 3/4 th catalyst bed layer are respectively introduced into the 1 st/2 nd, 2 nd/3 rd and 3 rd/4 th catalyst bed layer. The materials introduced between the catalyst beds are uniformly distributed along the section of the reactor by the 1 st/2 nd catalyst bed material distribution assembly 31, the 2 nd/3 rd catalyst bed material distribution assembly 32 and the 3 rd/4 th catalyst bed material distribution assembly 33 respectively and then enter the catalyst beds, so that a large number of uniformly distributed micro-size olefin droplets and micro-size water droplets exist in the reaction materials all the time, the miscibility of olefin/water is enhanced, the efficient mass transfer of olefin and water is realized, and the hydration reaction rate of olefin and the single-pass conversion rate of raw materials are greatly improved under the condition of lower water-olefin ratio.
The olefin hydration reactor and the olefin hydration reaction are respectively applied to the hydration reaction of n-butene and the hydration reaction of cyclohexene. Specific reaction conditions are shown in comparative examples 1, 2, 3, 4, 5 and 6. The n-butene and cyclohexene starting materials were commercially available, and the specific properties are shown in tables 1 and 2, respectively. Wherein, the catalyst adopted for the hydration of the n-butene is DNW-II type catalyst produced by Dandelion special resin Co., ltd, and the catalyst adopted for the hydration of the cyclohexene is amberlyst 36 type resin catalyst.
TABLE 1 n-butene feedstock composition
TABLE 2 cyclohexene raw material composition
Comparative example 1
N-butene in Table 1 was used as a starting material and was reacted with water in the presence of a catalyst to produce sec-butanol by hydration of n-butene. The normal butene raw material and water pass through a conventional static mixer with the model SL-1.6/25-10.0-250, are continuously mixed for three times, and the mixed material enters a normal butene hydration reactor to carry out hydration reaction. The reactor adopts a common up-flow reactor, three sections of catalyst beds are arranged in the reactor, a distribution sieve plate is arranged at the inlet of each section of catalyst bed, and the aperture of the sieve plate is 2mm. The mixing conditions were as follows: the temperature was 170℃and the pressure was 8.0MPa. Introducing n-butene/water mixture into an olefin hydration reactor from the bottom of the reactor, uniformly distributing the mixture along the section of the reactor through a distribution sieve plate, entering a catalyst bed layer for olefin hydration reaction, and finally leaving the olefin hydration reactor from a discharge hole at the top of the reactor
The reaction product is obtained by using the n-butene in the table 1 as a raw material through a n-butene hydration reactor, and the reaction conditions, the residence time and the conversion rate of the raw material are shown in the table 3.
Comparative example 2
Cyclohexene in Table 3 is used as a raw material, and is subjected to isobutene hydration reaction with water under the action of a catalyst to prepare tertiary butanol. The isobutene raw material and water pass through a conventional static mixer with the model SL-1.6/25-5 to 200, and the mixed material of the isobutene raw material and the water enters an isobutene hydration reactor to carry out hydration reaction. The reactor adopts a common up-flow reactor, three sections of catalyst beds are arranged in the reactor, a distribution sieve plate is arranged at the inlet of each section of catalyst bed, and the aperture of the sieve plate is 2.0mm. The mixing conditions were as follows: the temperature was 120℃and the pressure was 1.2MPa. The isobutene/water mixture is introduced into an olefin hydration reactor from the bottom of the reactor, uniformly distributed along the section of the reactor by a distribution sieve plate, enters a catalyst bed layer for olefin hydration reaction, and finally leaves the olefin hydration reactor from a discharge hole at the top of the reactor.
The cyclohexene in Table 2 was used as a raw material, and a reaction product was obtained by a cyclohexene hydration reactor, and the reaction conditions, residence time and conversion of the raw material were as shown in Table 3.
Example 1
N-butene in Table 1 was used as a starting material and was reacted with water in the presence of a catalyst to produce sec-butanol by hydration of n-butene. The olefin and water mixture I is introduced into a n-butene hydration reactor from the bottom of the reactor, and the hydration reactor is provided with three sections of catalyst beds. Introducing the mass ratio of the water and the olefin into the micro-channel mixing equipment I in a ratio of 5.0:1 to form a feed II, introducing the mass ratio of the water and the olefin into the micro-channel mixing equipment II in a ratio of 1:3 to form a feed III, introducing the feed II and the feed III between the first catalyst bed layer, the second catalyst bed layer and the third catalyst bed layer simultaneously, strengthening the intersolubility of the olefin and the water phase, realizing high-efficiency mass transfer, improving the single pass conversion rate of the olefin hydration reaction, and reducing the water and the olefin ratio. The reaction effluent leaves the reactor and enters the next separation unit. The mass ratio of the feed II to the feed III is 1:1.5; the mass of olefin in feed I is 75% of the total feed olefin mass, the mass of olefin in feed II is 10% of the total feed olefin mass, preferably 3% to 10%, and the mass of olefin in feed III is 15% of the total feed olefin mass.
The mass of the materials between the first catalyst bed, the second catalyst bed and the third catalyst bed, which are introduced by the feed II, is gradually decreased, and the decreasing proportion is 20%; the mass of the material between the first, second and third catalyst beds introduced by the feed III is gradually decreased by 20 percent. In the micro-channel mixing equipment I, the thin sheet in the micro-channel mixing component is made of stainless steel, the thickness of the thin sheet is 1.0mm, 5 layers of polypropylene fiber filaments with the diameter of 5 mu m and 2 layers of polypropylene fiber filaments with the diameter of 5 mu m are filled between the thin sheet cracks, the fiber filaments are distributed at equal intervals, the distance is 1 mu m, and the fiber filaments are in a curve shape with periodically changed wavy lines. In the micro-channel mixing equipment II, the thin sheet in the micro-channel mixing component is made of stainless steel, the thickness of the thin sheet is 1.0mm, 2 layers of polypropylene fiber filaments with the diameter of 5 mu m and 5 layers of polypropylene fiber filaments with the diameter of 5 mu m are filled between the thin sheet cracks, the fiber filaments are distributed at equal intervals, the distance is 1 mu m, and the fiber filaments are in curve shapes with periodically changed wavy lines. The operating conditions of the microchannel mixing device I were as follows: the temperature was 170℃and the pressure 7.2MPaG; the operating conditions of the microchannel mixing device II were as follows: the temperature was 170℃and the pressure 7.2MPaG.
The n-butene of Table 2 was used as a raw material, and the hydration reaction conditions, residence time and conversion of the raw material are shown in Table 3.
Example 2
In this example, the reaction materials, the reactor structure and the reaction process were the same as in example 1. Except that the mixed feed II and the mixed feed III formed by the microchannel mixing device I in this example were introduced from the second and third catalyst beds, respectively. Wherein, the operating conditions of the micro-channel mixing device I are as follows: the temperature was 170℃and the pressure 7.2MPaG; the operating conditions of the microchannel mixing device II were as follows: the temperature was 170℃and the pressure 7.2MPaG. The reaction conditions, residence times and conversion of the starting materials are shown in Table 3.
Example 3
In this example, the reaction materials, the reactor structure and the reaction process were the same as in example 1. Unlike example 1, this example employs more moderate reaction conditions, and the operating conditions of the microchannel mixing device I are as follows: the temperature was 148℃and the pressure was 6.0MPaG; the operating conditions of the microchannel mixing device II were as follows: the temperature was 148℃and the pressure was 6.0MPaG. The reaction conditions, residence times and conversion of the starting materials are shown in Table 3.
Example 4
Cyclohexene in Table 2 is used as a raw material, and is subjected to isobutene hydration reaction with water under the action of a catalyst to prepare tertiary butanol. After the mixture of olefin and water is fed into isobutene hydration reactor from the bottom of the reactor, and the hydration reactor is equipped with three catalyst beds. Introducing the mass ratio of the water and the olefin into the micro-channel mixing equipment I in a ratio of 7.0:1 to form a feed II, introducing the mass ratio of the water and the olefin into the micro-channel mixing equipment II in a ratio of 1:5 to form a feed III, introducing the feed II and the feed III between the first catalyst bed layer, the second catalyst bed layer and the third catalyst bed layer simultaneously, strengthening the intersolubility of the olefin and the water phase, realizing high-efficiency mass transfer, improving the single pass conversion rate of the olefin hydration reaction, and reducing the water and the olefin ratio. The reaction effluent leaves the reactor and enters the next separation unit. The mass ratio of the feed II to the feed III is 1:1; the mass of olefins in feed I was 78% of the total feed olefin mass, the mass of olefins in feed II was 8% of the total feed olefin mass, and the mass of olefins in feed III was 14% of the total feed olefin mass. The mass of the materials between the first catalyst bed, the second catalyst bed and the third catalyst bed, which are introduced by the feed II, is gradually decreased, and the decreasing proportion is 35%; the mass of the material between the first, second and third catalyst beds introduced by the feed III is gradually decreased by 25 percent.
In the micro-channel mixing equipment I, the thin sheet in the micro-channel mixing component is made of stainless steel, the thickness of the thin sheet is 1.5mm, 8 layers of polypropylene fiber filaments with the diameter of 5 mu m and 3 layers of polypropylene fiber filaments with the diameter of 5 mu m are filled between the thin sheet cracks, the fiber filaments are distributed at equal intervals, the distance is 1 mu m, and the fiber filaments are in a curve shape with periodically changed wavy lines. In the micro-channel mixing equipment II, the thin sheet in the micro-channel mixing component is made of stainless steel, the thickness of the thin sheet is 1.5mm, 3 layers of polypropylene fiber filaments with the diameter of 5 mu m and 8 layers of polypropylene fiber filaments with the diameter of 5 mu m are filled between the thin sheet cracks, the fiber filaments are distributed at equal intervals, the distance is 1 mu m, and the fiber filaments are in a curve shape with periodically changed wavy lines. The operating conditions of the microchannel mixing device I were as follows: the temperature is 120 ℃ and the pressure is 1.2MPaG; the operating conditions of the microchannel mixing device II were as follows: the temperature was 120℃and the pressure 1.2MPaG.
Cyclohexene of Table 2 was used as a starting material, and the hydration reaction conditions, residence time and conversion of the starting material are shown in Table 3.
Example 5
In this example, the reaction materials, the reactor structure and the reaction process were the same as in example 4. Unlike example 4, the mixed feed II and the mixed feed III formed by the microchannel mixing device I in this example were introduced from the second and third catalyst beds, respectively. Wherein, the operating conditions of the micro-channel mixing device I are as follows: the temperature is 120 ℃ and the pressure is 1.2MPaG; the operating conditions of the microchannel mixing device II were as follows: the temperature was 120℃and the pressure 1.2MPaG. The reaction conditions, residence times and conversion of the starting materials are shown in Table 3.
Example 6
In this example, the reaction materials, the reactor structure and the reaction process were the same as in example 4. Unlike example 4, this example employs more moderate reaction conditions, and the operating conditions of the microchannel mixing device I are as follows: the temperature was 105℃and the pressure was 1.0MPaG; the operating conditions of the microchannel mixing device II were as follows: the temperature was 105℃and the pressure was 1.0MPaG. The reaction conditions, residence times and conversion of the starting materials are shown in Table 3.
Example 7
N-butene in Table 1 was used as a starting material and was reacted with water in the presence of a catalyst to produce sec-butanol by hydration of n-butene. The olefin and water mixture I is introduced into a n-butene hydration reactor from the bottom of the reactor, and the hydration reactor is provided with three sections of catalyst beds. Introducing the mass ratio of the water and the olefin into a jet mixer A to form a feed II in a ratio of 4.5:1, introducing the mass ratio of the water and the olefin into the jet mixer A to form a feed III in a ratio of 1:2.0, introducing the feed II and the feed III between the first catalyst bed layer, the second catalyst bed layer and the third catalyst bed layer at the same time, strengthening the intersolubility of the olefin and the water, realizing high-efficiency mass transfer, improving the single-pass conversion rate of the olefin hydration reaction, and reducing the water and the olefin ratio. The reaction effluent leaves the reactor and enters the next separation unit. The mass ratio of the feed II to the feed III is 1:2.0; the mass of olefins in feed I was 70% of the total feed olefin mass, the mass of olefins in feed II was 15% of the total feed olefin mass, and the mass of olefins in feed III was 15% of the total feed olefin mass. The mass of the materials between the first catalyst bed, the second catalyst bed and the third catalyst bed, which are introduced by the feed II, is gradually decreased, and the decreasing proportion is 15%; the mass of the material between the first, second and third catalyst beds introduced by the feed III is gradually decreased by 15 percent.
The normal butene of Table 1 was used as the raw material, and the hydration reaction conditions, residence time and single pass conversion of the raw material were shown in Table 3.
Example 8
Cyclohexene in Table 2 is used as a raw material, and is subjected to isobutene hydration reaction with water under the action of a catalyst to prepare tertiary butanol. After the mixture of olefin and water is fed into isobutene hydration reactor from the bottom of the reactor, and the hydration reactor is equipped with three catalyst beds. Introducing the mass ratio of the water and the olefin into the jet mixer A in a ratio of 7.5:1 to form a feed II, introducing the mass ratio of the water and the olefin into the jet mixer B in a ratio of 1:6.0 to form a feed III, introducing the feed II and the feed III between the first catalyst bed layer, the second catalyst bed layer and the third catalyst bed layer simultaneously, strengthening the intersolubility of the olefin and the water phase, realizing high-efficiency mass transfer, improving the single pass conversion rate of the olefin hydration reaction and reducing the water and the olefin ratio. The reaction effluent leaves the reactor and enters the next separation unit. The mass ratio of the feed II to the feed III is 1:1; the mass of olefins in feed I was 80% of the total feed olefin mass, the mass of olefins in feed II was 10% of the total feed olefin mass, and the mass of olefins in feed III was 10% of the total feed olefin mass. The mass of the materials between the first catalyst bed, the second catalyst bed and the third catalyst bed, which are introduced by the feed II, is gradually decreased, and the decreasing proportion is 15%; the mass of the material between the first, second and third catalyst beds introduced by the feed III is gradually decreased by 15 percent.
The cyclohexene of Table 2 was used as a starting material, and the hydration reaction conditions, residence time and single pass conversion of the starting material are shown in Table 3.
TABLE 3 reaction conditions and results
The dispersion size and the dispersion effect of the olefin liquid drops in water in the method are obtained through a high-speed camera, and the uniformity of dispersed phase particles is obtained through selecting a plurality of characteristic particles, so that the smaller the particle size is, the higher the uniformity is, and the better the mixing and dispersion effect is. For this reason, the method for measuring the mixing and dispersing effect of the present example and comparative example is as follows: under the same condition, mixing the disperse phase olefin and the continuous phase water phase by different mixing and dispersing methods (such as a conventional static mixer, a micro-channel mixing device I and a micro-channel mixing device II in the reactor), at least 10 groups of mixed material samples are obtained by each group of methods, the particle size of the disperse phase in the mixed material samples is shot by using a British IX I-SPEED 5 high-SPEED camera, the particles in the photo are added, the percentage content of the particles with various sizes is calculated, and a normal distribution diagram of the particles with various sizes is obtained, so that the particle uniformity is obtained.
As can be seen from the mixing effect of the embodiment and the comparative example, by adopting the olefin hydration reaction method, partial olefin and water form a mixed material I reaction material which is introduced from the bottom of the reactor, then partial olefin and water form mixed feed II through the micro-channel mixing equipment I under the condition that the water-to-olefin ratio is more than or equal to 1, olefin is dispersed in water in a micro-size liquid drop mode, the reactor is introduced from between catalyst beds, the other part of olefin and water form mixed feed III through the micro-channel mixing equipment II under the condition that the water-to-olefin ratio is less than 1, water is dispersed in olefin in a micro-size liquid drop mode, and the reactor is introduced from between the catalyst beds, so that a large amount of uniformly distributed micro-size olefin liquid drops and micro-size liquid drops can be always present in the reaction material, the intersolubility of olefin and water is enhanced, the efficient mass transfer of olefin and water is realized, the olefin hydration reaction rate and the single-pass conversion rate of raw material are greatly improved under the condition that the water-to-olefin ratio is lower, the number and the volume of the reactor are reduced, and the energy consumption in the separation process is reduced.
Claims (21)
1. An olefin hydration reaction method, which is characterized by comprising the following steps: a plurality of catalyst beds are arranged in the olefin hydration reactor, and the catalyst beds are the 1 st to the n th catalyst beds from bottom to top in sequence; dividing a reaction mixture comprising an olefin phase and an aqueous phase into a feed I, a feed II and a feed III; feeding I enters a 1 st catalyst bed layer from the bottom of an olefin hydration reactor, feeding II is divided into x strands after mixing and dispersing, different catalyst beds are introduced between the catalyst beds, feeding III is divided into y strands after mixing and dispersing, different catalyst beds are introduced between the catalyst beds, and at least 1 strand of material in the x strands of feeding II and at least 1 strand of material in the y strands of feeding III are introduced into the same catalyst bed; each feed is subjected to olefin hydration reaction in the catalyst bed, and the final reaction product flows out from the top of the reactor and enters the next separation unit; wherein the water-to-olefin ratio of the feed II is more than or equal to 1, and the water-to-olefin ratio of the feed III is less than 1; the x is less than n, y is less than n, and n is more than or equal to 2; the water-olefin ratio is the mass ratio of the water phase to the olefin phase; the mixing and dispersing of the feed II and the feed III adopts a micro-channel mixing device, and the micro-channel mixing device comprises a shell and at least one micro-channel mixing component; the micro-channel component is fixed in the shell, one end of the shell is provided with an inlet for feeding the olefin phase and the water phase, and the other end of the shell is provided with an outlet for outflow of the mixed materials; the micro-channel assembly in the shell is divided into a feeding end and a discharging end along the crack direction, and other ends except the feeding end and the discharging end of the micro-channel assembly are hermetically connected with the shell; the microchannel mixing assembly comprises a plurality of stacked sheets and lipophilic and/or hydrophilic fiber filaments filled between seams of adjacent sheets; the fiber filaments form a plurality of micro-channels, and are clamped and fixed by the thin sheet; the fiber filaments filled between the seams of the adjacent sheets are arranged in a single layer or multiple layers.
2. The method according to claim 1, characterized in that: the water-to-olefin ratio of the feed II is 1:1-10:1, and the water-to-olefin ratio of the feed III is 1:1.5-1:10.
3. The method according to claim 1, characterized in that: and n is less than or equal to 10.
4. The method according to claim 1, characterized in that: and n is less than or equal to 5.
5. The method according to claim 1, characterized in that: said x=y.
6. The method according to claim 1, characterized in that: the mass of olefin in the feed I accounts for 30% -98% of the total mass of olefin in the feed; the mass of the olefin in the feed II accounts for 1-35% of the total feed olefin mass, and the mass of the olefin in the feed III accounts for 1-35% of the total feed olefin mass; wherein the total feed olefin mass is the total mass of olefins in feed I, feed II and feed III.
7. The method according to claim 1, characterized in that: the mass ratio of the total water to the alkene is 1:1-20:1.
8. The method according to claim 1, characterized in that: the mass ratio of the total water to the alkene is 1:1-15:1.
9. The method according to claim 1, characterized in that: the feed I is mixed by adopting premixing equipment with a mixing function and is selected from one or more of static mixers, stirred tanks, colloid mills or inorganic membrane tubes.
10. The method according to claim 1, characterized in that: the olefin is one or more of ethylene, propylene, n-butene, isobutene, isoamylene or cyclohexene.
11. The method according to claim 1, characterized in that: the olefin hydration reactor is a fixed bed reactor, one or more olefin hydration reactors are arranged, and the olefin hydration reactors are connected in series or in parallel.
12. The method according to claim 1, characterized in that: the mass ratio of the feed II to the feed III is 1:50-50:1.
13. The method according to claim 1, characterized in that: and after the feed II and the feed III enter the reactor, the feed II and the feed III are uniformly distributed on the section of the reactor, and the material distribution assembly is arranged in the reactor.
14. The method according to claim 1, characterized in that: the dispersion size of olefin liquid drops in the feed II reaches 0.5-900 mu m, and the dispersion size of water phase liquid drops in the feed III reaches 0.5-900 mu m.
15. The method according to claim 1, characterized in that: when the fiber filaments are arranged in multiple layers, the projection of two adjacent layers of fiber filaments along the vertical direction of the sheet is of a net structure; in each layer of fiber filaments, the distance between adjacent fiber filaments is 0.5-50 μm.
16. The method according to claim 1, characterized in that: the thickness of the thin sheet is 0.05 mm-5 mm; the sheet material is any one of metal, ceramic, organic glass or polyester material.
17. The method according to claim 1, characterized in that: the lipophilic fiber yarn is at least one selected from polyester fiber yarn, nylon fiber yarn, polyurethane fiber yarn, polypropylene fiber yarn, polyacrylonitrile fiber yarn and polyvinyl chloride fiber yarn, or fiber yarn with surface subjected to lipophilic treatment by a physical or chemical method; the hydrophilic fiber yarn is selected from high molecular polymers with main chains or side chains containing carboxyl, amido, amino or hydroxyl hydrophilic groups, or fiber yarn obtained by hydrophilic treatment of materials by physical or chemical methods.
18. The method according to claim 1, characterized in that: when the olefin phase is a disperse phase, the ratio of the lipophilic fiber filaments to the hydrophilic fiber filaments filled among the micro-channel sheets is 50:1-1:1; in the feed II after mixing and dispersing by the micro-channel mixing equipment, the dispersion size d1 of olefin liquid drops is 0.5-900 mu m, and the dispersion uniformity is more than or equal to 80%.
19. The method according to claim 1, characterized in that: when the water phase is a disperse phase, the ratio of the lipophilic fiber filaments to the hydrophilic fiber filaments filled among the micro-channel sheets is 1:1-1:50; in the feed III after mixing and dispersing by the micro-channel mixing equipment, the dispersion size d1 of the water drops is 0.5-900 mu m, and the dispersion uniformity is more than or equal to 80%.
20. The method according to claim 1, characterized in that: in the x strands divided by the feed II, the mass of each strand of material flow decreases along the material flow direction, and the decreasing proportion is 3-80%.
21. The method according to claim 1, characterized in that: in the y strands of the feed III, the mass of each strand of material flow decreases along the material flow direction, and the decreasing proportion is 3-80%.
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