阅读说明：本技术 一种烯烃水合反应方法和系统 (Olefin hydration reaction method and system ) 是由 袁清 毛俊义 黄涛 朱振兴 秦娅 唐晓津 郑博 于 2019-10-14 设计创作，主要内容包括：一种烯烃水合反应方法,将水与混合碳四原料分别引入反应器,与固体酸催化剂混合并接触,在水合反应条件下进行水合反应得到叔丁醇；烯烃水合反应装置由反应器(5)、液固分离器(10)、液液分离器(15)和喷射混合器(4)组成,其中,所述的反应器底部设有分散相入口(1)和连续相入口,所述的反应器顶部依次经下降管上段(9)、固液分离器、下降管下段(11)、喷射混合器(4)与反应器底部连通,所述的固液分离器的清液出口(12)与所述的液液分离器入口连通,所述的液液分离器的水相出口与所述的喷射混合器(4)的吸入口连通。本发明提供的烯烃水合反应方法强化了液液传质,实现了催化剂在反应器内循环流动,能够提高反应效率和实现装置的长周期运行。(A method for olefin hydration reaction, respectively introducing water and mixed C-C raw materials into a reactor, mixing and contacting with a solid acid catalyst, and carrying out hydration reaction under the hydration reaction condition to obtain tert-butyl alcohol; the olefin hydration reaction device consists of a reactor (5), a liquid-solid separator (10), a liquid-liquid separator (15) and a jet mixer (4), wherein the bottom of the reactor is provided with a dispersed phase inlet (1) and a continuous phase inlet, the top of the reactor is communicated with the bottom of the reactor through a downcomer upper section (9), the solid-liquid separator, a downcomer lower section (11) and the jet mixer (4) in sequence, a clear liquid outlet (12) of the solid-liquid separator is communicated with the inlet of the liquid-liquid separator, and a water phase outlet of the liquid-liquid separator is communicated with a suction inlet of the jet mixer (4). The olefin hydration reaction method provided by the invention strengthens liquid-liquid mass transfer, realizes the circular flow of the catalyst in the reactor, and can improve the reaction efficiency and realize the long-period operation of the device.)

1. A method for olefin hydration reaction, introduce water and mixed C four raw materials containing isobutene into reactor through disperse phase entry and continuous phase entry separately, the water oil two-phase mixes and contacts with solid acid catalyst, carry on the hydration reaction under the hydration reaction condition, the material flow separates and gets tertiary butanol after the reaction; the adopted olefin hydration reaction device consists of a reactor (5), a liquid-solid separator (10), a liquid-liquid separator (15) and a jet mixer (4), wherein the bottom of the reactor is provided with a dispersed phase inlet (1), a continuous phase inlet and a catalyst discharge outlet (8), the top of the reactor is communicated with the bottom of the reactor through a downcomer upper section (9), the solid-liquid separator, a downcomer lower section (11) and the jet mixer (4) in sequence, a clear liquid outlet (12) of the solid-liquid separator is communicated with the inlet of the liquid-liquid separator, a water phase outlet of the liquid-liquid separator is communicated with a first suction inlet of the jet mixer (4), and the liquid-liquid separator is also provided with an oil phase outlet (16).

2. The olefin hydration reaction process of claim 1 where the isobutylene content of the mixed C4 feedstock is in the range of 5 wt% to 50 wt%; the volume flow ratio of the water to the mixed carbon four is (0.1-2) to 1; the particle diameter of the solid acid catalyst is 0.05-3.0 mm.

3. A process for the hydration of olefins according to claim 1 or 2, characterized in that the hydration conditions are: the reaction temperature is 30-100 deg.C, the pressure is 0.3-3.0MPa, preferably 40-80 deg.C, and the pressure is 0.6-2.0 MPa.

4. A process for the hydration of olefins according to claim 1, characterized in that the dispersed phase inlet (1) is provided with a dispersed phase feeder (2) which is a perforated pipe, a sintered metal pipe, an inorganic membrane pipe or an atomizing nozzle.

5. The system hydration reaction method of claim 4, wherein the pressure drop before and after the dispersed phase feeder 2 is 0.05 to 3.0MPa, and the initial liquid flow rate at the outlet of the dispersed phase feeder is 5 to 40 m/s.

6. A process for the hydration of olefins according to claim 1 or 2, wherein the solid acid catalyst is selected from solid phosphoric acid, strong acid cation exchange resins, molecular sieve catalysts or heteropolyacid catalysts.

7. The olefin hydration process of claim 1 where the liquid hourly space velocity of the mixed carbon-four feed relative to the total catalyst inventory in the reactor is in the range of 0.1 to 5 hours^-1Preferably 0.5 to 3 hours^-1。

8. A process for the hydration of olefins according to claim 1, characterized in that said reactor comprises a lower straight section (5) and an upper enlarged section (7), said straight section (5) being provided with at least one draft tube (6) dividing the internal space of said straight section into an ascending zone (I) and a descending zone (II).

9. A process for the hydration of olefins according to claim 8, wherein the ratio of the diameter of the counter-expansion section to the diameter of the straight section is (1.2-5): 1, preferably (1.6-3): 1; the height ratio of the expanding section to the straight pipe section is (0.1-0.6): 1, preferably (0.2 to 0.4): 1.

10. the olefin hydration reaction process of claim 8, wherein the ratio of the cross-sectional area of the ascending zone to the descending zone in the straight pipe section is (0.2 to 3):1, preferably (0.3-2): 1.

11. the process for the hydration of olefins according to claim 8, wherein a dispersed phase feeder is provided at the bottom of each draft tube.

12. The process for the hydration of olefins according to claim 1, wherein said downcomer has an upper section and a lower section having the same internal diameter, and the ratio of the diameters of the downcomer and the reactor straight section is (0.3 to 5):1, preferably (0.5 to 3): 1.

13. the olefin hydration reaction method according to claim 1, wherein the liquid-solid separator is a filter assembly, the filter assembly comprises a shell and a filter pipe, and the filter pipe is one or a combination of several of an inorganic ceramic membrane, a metal pipe membrane, a metal screen and a metal sintering pipe.

14. A method of hydrating olefins according to claim 13, wherein the filter assembly housing further comprises a catalyst inlet.

15. The process for the hydration of olefins according to claim 13, wherein the filter assembly is provided with a backwash line.

16. The olefin hydration reaction process of claim 1, wherein the lower section of the downcomer is in communication with the second suction inlet of the eductor and the aqueous phase outlet of the liquid-liquid separator is in communication with the first suction inlet of the eductor.

17. The process for the hydration of olefins according to claim 1, wherein the liquid-liquid separator is selected from one or a combination of conventional gravity settling tanks, coalescer separators and fibrous membrane surface separators.

18. An olefin hydration reaction system is characterized by comprising an olefin hydration reaction device and a reaction system consisting of water-oil two-phase and solid acid catalyst particles, wherein the water phase is deionized water and reaction product tert-butyl alcohol, the oil phase is a mixed carbon-four raw material containing isobutene, the particle size of the solid acid catalyst particles is 0.05-3.0 mm, the olefin hydration reaction device consists of a reactor (5), a liquid-solid separator (10), a liquid-liquid separator (15) and a jet mixer (4), wherein the bottom of the reactor is provided with a dispersed phase inlet (1), a continuous phase inlet and a catalyst discharge outlet (8), the top of the reactor is communicated with the bottom of the reactor through an upper descending pipe section (9), a solid-liquid separator, a lower descending pipe section (11) and the jet mixer (4) in sequence, a clear liquid outlet (12) of the solid-liquid separator is communicated with the inlet of the liquid-liquid separator, the water phase outlet of the liquid-liquid separator is communicated with the first suction port of the jet mixer (4), and the liquid-liquid separator is also provided with an oil phase outlet (16).

Technical Field

The invention relates to equipment and a method for preparing tert-butyl alcohol, in particular to equipment and a corresponding method for preparing tert-butyl alcohol by taking solid acid as a catalyst and isobutene and deionized water in a carbon-four mixture as raw materials.

Technical Field

Tert-butyl alcohol (TBA) is an important chemical product, is mainly used as a solvent and an intermediate for preparing compounds such as methyl methacrylate, tert-butyl phenol, tert-butylamine and the like, and can also be used as an intermediate for purifying isobutene from a carbon-four mixture. The industrial synthesis of tert-butanol is mainly obtained by the addition reaction of water and isobutene under the action of an acid. The liquid sulfuric acid method has been gradually replaced by the solid resin method due to serious corrosion, low product purity and the like. However, because water and carbon four are immiscible systems, the flow and distribution of materials in the reactor are very uneven, and the conversion rate of olefin is further influenced, and the conversion rate of reaction under the conventional cocurrent operation condition can only reach about 50%.

In order to increase the conversion of isobutene water and reaction, the following methods are mainly adopted: (1) changing the flow state of the materials in the reactor and strengthening the phase-to-phase contact, for example, CN 1108203A discloses a method for preparing tertiary butanol, and reaction power is increased by the countercurrent contact of isobutene and water, thereby improving reaction conversion rate. However, the main problem is the high catalyst requirement, and the packing type is required to provide sufficient fluid passage and contact area, so the cost is high. (2) The mutual solubility of water and carbon four is improved by adding a cosolvent. For example CN 101293813A with emulsifier RC₆H₅O(CH₂CH₂O)_nH, forming water-in-water oil emulsion by the four carbon components and water, and then carrying out hydration reaction, wherein the conversion rate of isobutene can be improved to about 70%. However, the addition of such non-raw materials may cause a series of side reactionsAnd has great influence on subsequent separation and product purity. In addition, in the conventional means, for strengthening the liquid-liquid mixing process, methods generally adopted in industry include mechanical stirring, design of a tortuous flow passage, high-speed impact of liquid and the like, and the purpose of the method is to generate fluid turbulence so as to increase the mixing efficiency of the liquid. The most common reactor is a stirred tank, which utilizes the mechanical stirring action of a stirrer to realize the mixing and reaction of raw materials. However, due to the limitation of the stirred tank device, the mixing time scale is between several minutes and even several hours, and the mixing time scale is usually used for reaction systems with slower reaction rate. For example, CN 202527171a discloses a reaction apparatus for gas-liquid-solid heterogeneous reaction, in which a guide shell is installed inside a reactor, and a stirrer is installed inside the guide shell, and the contact reaction of raw materials is realized by means of stirring. The conventional pipeline static mixer adopts a tortuous flow passage to perform intensified mixing on fluid, but the mixing effect is relatively poor.

For the use of solid phase catalyst, the catalyst is mostly filled in a fixed bed form at present, and the method is characterized in that the filling of the catalyst is difficult, and the components in the reactor are complex; in addition, the catalyst particles are relatively large and are not beneficial to contact reaction with a liquid-liquid phase, so that the reaction efficiency is low. In the method disclosed in CN 101314596a, the catalyst is made into slurry with one of the liquid phases to react, which improves the catalytic efficiency, but the method has the disadvantages that the catalyst and the product need to be separated, and the catalyst particles are too small, which results in a complicated separation process and a short back-washing period of the filter device.

Disclosure of Invention

The invention aims to solve the technical problem of providing a method for preparing tertiary butanol by taking solid acid as a catalyst and isobutene and deionized water in a carbon-four mixture as raw materials on the basis of the prior art.

A water and reaction method of olefin, introduce water and mixed C four raw materials containing isobutene into reactor through disperse phase feed inlet and continuous phase feed inlet separately, two phases contact and mix with solid acid catalyst, carry on the hydration reaction under the condition of hydration reaction, the material flow separates and gets tertiary butanol after the reaction; the adopted olefin hydration reaction device consists of a reactor 5, a liquid-solid separator 10, a liquid-liquid separator 15 and a jet mixer 4, wherein the bottom of the reactor is provided with a dispersed phase inlet 1, a continuous phase inlet and a catalyst discharge outlet 8, the top of the reactor is communicated with the bottom of the reactor through a downcomer upper section 9, the solid-liquid separator, a downcomer lower section 11 and the jet mixer 4 in sequence, a clear liquid outlet 12 of the solid-liquid separator is communicated with the inlet of the liquid-liquid separator, a water phase outlet of the liquid-liquid separator is communicated with a first suction inlet of the jet mixer 4, and the liquid-liquid separator is also provided with an oil phase outlet.

An olefin hydration reaction system comprises an olefin hydration reaction device and a reaction system consisting of a water-oil two-phase and solid acid catalyst particles, wherein the water phase is deionized water and reaction product tert-butyl alcohol, the oil phase is a mixed carbon-four raw material containing isobutene, the particle size of the solid acid catalyst particles is 0.05-3.0 mm, the olefin hydration reaction device consists of a reactor 5, a liquid-solid separator 10, a liquid-liquid separator 15 and a jet mixer 4, wherein the bottom of the reactor is provided with a dispersed phase inlet 1, a continuous phase inlet and a catalyst discharge outlet 8, the top of the reactor is communicated with the bottom of the reactor sequentially through an upper pipe section 9, a solid-liquid separator, a lower pipe section 11 and a jet mixer 4, a clear liquid outlet 12 of the solid-liquid separator is communicated with the inlet of the liquid-liquid separator, a water phase outlet of the liquid-liquid separator is communicated with a first suction inlet of the jet mixer 4, the liquid-liquid separator is also provided with an oil phase outlet.

The olefin water and the reaction method provided by the invention have the beneficial effects that:

compared with the prior art, the alkene water and the reaction method provided by the invention adopt a special reaction device, disperse a phase reactant into micro liquid through a dispersed phase feeder, and simultaneously form internal circulation in the reactor in the mixing reaction process, so that the liquid-solid mixing is enhanced to meet the requirement of hydration reaction. (1) Other surfactants or cosolvents are not required to be added into the reaction system, stirring equipment is not required in the reactor, and the reaction efficiency is higher. (2) The solid acid catalyst with the particle size between that of the fixed bed and that of the slurry bed can reduce the influence of surface diffusion and inner diffusion of the catalyst on the reaction to some extent, and is easier to realize liquid-solid separation compared with the slurry catalyst. (3) Because the solid phase catalyst is in a circulating flow state in the reactor, the catalyst is easy to load and unload, and the catalyst can be updated on line, thereby prolonging the shutdown and overhaul period of the device. (3) Can realize the full circulation of the water phase and has no discharged wastewater in the whole process.

Drawings

FIG. 1 is a schematic flow diagram of a process for the hydration reaction of olefins.

FIG. 2 is a schematic structural view of a fiber membrane separator used in the examples.

1-dispersed phase inlet; 2-dispersed phase feeder; 3-a continuous phase inlet; 4-a jet mixer; 5-a straight pipe section; 6-a flow guide pipe; 7-an expansion section; 8-catalyst discharge port; 9-upper section of downcomer; 10-liquid-solid separator; 11-lower section of downcomer; 12-clear liquid outlet; 13-catalyst inlet; 14-backwash liquid; 15-liquid separator; 16-oil phase outlet; 17-a water phase outlet; i-a rising zone; II-a liquid descending zone.

Detailed Description

The following describes in detail specific embodiments of the present invention.

A water and reaction method of olefin, introduce water and mixed C four raw materials containing isobutene into reactor through disperse phase feed inlet and continuous phase feed inlet separately, two phases contact and mix with solid acid catalyst, carry on the hydration reaction under the condition of hydration reaction, the material flow separates and gets tertiary butanol after the reaction; the adopted olefin hydration reaction device consists of a reactor 5, a liquid-solid separator 10, a liquid-liquid separator 15 and a jet mixer 4, wherein the bottom of the reactor is provided with a raw material inlet 1 and a catalyst discharge outlet 8, the top of the reactor is communicated with the bottom of the reactor through a downcomer upper section 9, the solid-liquid separator, a downcomer lower section 11 and the jet mixer 4 in sequence, a clear liquid outlet 12 of the solid-liquid separator is communicated with an inlet of the liquid-liquid separator, a water phase outlet of the liquid-liquid separator is communicated with a first suction inlet of the jet mixer 4, and the liquid-liquid separator is also provided with an oil phase outlet.

In the olefin hydration reaction method provided by the invention, the mixed carbon four raw material is from mixed carbon four produced by different devices, and the content of isobutene in the mixed carbon four raw material is 5-50 wt%; the volume flow ratio of water to the mixed C4 is (0.1-2): 1, preferably, the water comprises fresh water and circulating water after liquid-liquid separation; the liquid hourly space velocity of the mixed carbon four raw material relative to the total inventory of the catalyst in the reactor is 0.1-5 h^-1Preferably 0.5 to 3 hours^-1. The particle diameter of the solid acid catalyst is 0.05-3.0 mm, and the particle density is 0.6-1.5 g/mL.

In the olefin hydration reaction method provided by the invention, the hydration reaction conditions are as follows: the reaction temperature is 30-100 ℃, and preferably 40-80 ℃; the pressure is 0.3-3.0MPa, preferably 0.6-2.0 MPa.

In the olefin hydration reaction method provided by the invention, the solid acid catalyst is selected from solid phosphoric acid, strong acid cation exchange resin, a molecular sieve catalyst or a heteropolyacid catalyst. More preferably a strong acid type ion exchange resin catalyst.

In the olefin hydration reaction device, the reactor consists of a lower straight pipe section 5 and an upper expanding section 7, at least one guide pipe 6 is arranged in the straight pipe section 5, and the internal space of the straight pipe section is divided into an ascending area I and a descending area II.

Preferably, the diameter ratio of the reverse expansion section to the straight pipe section is (1.2-5) to 1, more preferably (1.6-3) to 1; the height ratio of the expanding section to the straight pipe section is (0.1-0.6): 1, preferably (0.2 to 0.4): 1.

preferably, the cross-sectional area ratio of the ascending area to the descending area in the straight pipe section is (0.2-3): 1, preferably (0.3-2): 1.

preferably, the raw material inlet 1 is provided with a disperse phase feeder 2, and the disperse phase feeder is a porous pipe, a sintered metal pipe, an inorganic membrane pipe or an atomizing nozzle. And in the case that the straight pipe section is provided with a plurality of flow guide pipes, the bottom of each flow guide pipe is provided with a dispersed phase feeder.

Preferably, the inner diameters of the upper section of the downcomer and the lower section of the downcomer are the same, and the ratio of the inner diameters of the downcomer and the straight pipe section is (0.3-5): 1, preferably (0.5 to 3): 1.

preferably, the liquid-solid separator is a filtering assembly, the filtering assembly comprises a shell and a filtering pipe, and the filtering pipe is one or a combination of several of an inorganic ceramic membrane, a metal pipe membrane, a metal screen and a metal sintering pipe.

Preferably, the filter assembly shell is also provided with a catalyst feeding port.

Preferably, a back washing pipeline is arranged on the filtering component.

Preferably, the lower downcomer section is communicated with the second suction port of the jet mixer, and the water phase outlet of the liquid-liquid separator is communicated with the first suction port of the jet mixer. The jet mixer is provided with a first suction port, a second suction port and a jet port, wherein the first suction port is a high-speed jet fluid inlet, and the second suction port is a main fluid inlet. In the reaction process, the flow velocity of the high-speed jet fluid at the jet outlet of the jet mixer is 3-30 m/s.

Preferably, the first suction port of the jet mixer is also connected to the continuous phase inlet to replenish water during the reaction.

Preferably, the liquid-liquid separator is selected from one or a combination of a conventional gravity settling tank, an oil-water coalescence separator and a fiber membrane surface separator.

In the olefin hydration reaction device, at least one guide pipe 6 is arranged in a straight pipe section at the lower part of the reactor, and the internal space of the straight pipe section is divided into an ascending area I and a descending area II. When a plurality of guide pipes are arranged, as shown in the attached figure 2, the guide pipes are uniformly distributed in the straight pipe section, and the inner space of the straight pipe section is divided into an ascending area I and a descending area II.

And a disperse phase feeder 2 is arranged at the disperse phase inlet, and when a plurality of guide pipes are arranged in the straight pipe section, a disperse phase feeder is arranged at the bottom of each guide pipe. In the olefin hydration reaction, the dispersed phase can be oil phase or water phase, and the dispersed phase feeder is a porous pipe, a sintered metal pipe, an inorganic membrane pipe or an atomizing nozzle. The dispersed phase feeder has a remarkable throttling effect, and the optimal range of the pressure difference between the front and the back of the feeder is required to be 0.05-3.0 MPa, and the liquid flow rate of a feeding port is 5-40 m/s.

One or more than one downcomer is/are arranged, one end of the downcomer is connected with the top end of the reactor, and the other end of the downcomer is connected with the bottom of the reactor to form a circulation loop. Preferably, the inner diameters of the upper section of the downcomer and the lower section of the downcomer are the same, and the diameter ratio of the downcomer to the straight pipe section of the reactor is (0.3-5): 1, preferably (0.5 to 3): 1.

the upper section of the downcomer is communicated with a liquid-solid separator, and the liquid-solid separator is preferably a filtering assembly and is used for carrying out liquid-solid separation on materials from the top of the reactor. The filter component comprises a shell and a filter pipe, wherein the filter pipe is selected from one or a combination of several of an inorganic ceramic membrane, a metal pipe membrane, a metal screen mesh, a metal sintering pipe and the like. The filter components can be one or more groups. The filtration assembly is provided with a clear liquid outlet and a trapped liquid outlet, the clear liquid outlet is communicated with the liquid-liquid separator, the trapped liquid outlet is communicated with the bottom of the reactor through the lower section of the downcomer, and the trapped liquid is used as a circulating material and returns to the bottom of the reactor through the jet mixer in the use process.

The filter assembly is provided with a filter backwash inlet, and a preferable backwash inlet pipeline and a clear liquid outlet pipeline obtained by liquid-solid separation share one interface on the shell of the filter assembly. The backwash liquid is selected from the group consisting of a filtered supernatant or a fresh feed solution.

The lower section of the downcomer is communicated with the jet mixer. And the circulating material from the trapped liquid outlet of the liquid-solid separator is used as the suction fluid of the jet mixer, the raw material from the continuous phase inlet and the circulating liquid phase from the water phase outlet 17 of the liquid-liquid separator are used as high-speed jet fluid, and the jet flow speed is preferably 3-30 m/s. The two materials are mixed by the jet mixer 4 and then enter the bottom of the reactor.

The olefin hydration reaction method provided by the invention adopts the granular solid acid catalyst which is added into the reaction device through the catalyst adding port 13 arranged on the liquid-solid separator 10. As the abrasion and the inactivation of a part of catalyst are inevitably caused in the reaction process, in order to ensure the overall activity of the catalyst, the activity and the abrasion condition of the catalyst need to be regularly inspected, and a part of catalyst is discharged from a catalyst discharge port 8 at the bottom of the straight pipe section of the reactor, so that the online updating of the catalyst is realized, and the influence on the operation period of the device caused by the shutdown of the device is avoided.

An olefin hydration reaction system comprises an olefin hydration reaction device and a reaction system consisting of water-oil two-phase and solid acid catalyst particles, wherein the water phase is deionized water and reaction product tert-butyl alcohol, the oil phase is a mixed carbon-four raw material containing isobutene, the particle size of the solid acid catalyst particles is 0.05-3.0 mm, the olefin hydration reaction device consists of a reactor 5, a liquid-solid separator 10, a liquid-liquid separator 15 and a jet mixer 4, wherein the bottom of the reactor is provided with a dispersed phase inlet 1, a continuous phase inlet and a catalyst discharge outlet 8, the top of the reactor is communicated with the bottom of the reactor sequentially through an upper pipe section 9, a solid-liquid separator, a lower pipe section 11 and a jet mixer 4, a clear liquid outlet 12 of the solid-liquid separator is communicated with the inlet of the liquid-liquid separator, a water phase outlet of the liquid-liquid separator is communicated with the inlet of the jet mixer 4, the liquid-liquid separator is also provided with an oil phase outlet.

The olefin hydration reaction process and system of the present invention will be further described with reference to the accompanying drawings. But not to limit the invention accordingly.

FIG. 1 is a schematic flow diagram of a process for the hydration reaction of olefins. As shown in the attached figure 1, the adopted olefin water and reaction device comprises a reactor 5, a liquid-solid separator 10, a liquid-liquid separator 15 and a jet mixer 4, wherein the bottom of the reactor is provided with a raw material inlet 1 and a catalyst discharge outlet 8, the top of the reactor is communicated with the bottom of the reactor through a downcomer upper section 9, the solid-liquid separator, a downcomer lower section 11 and the jet mixer 4 in sequence, a clear liquid outlet 12 of the solid-liquid separator is communicated with an inlet of the liquid-liquid separator, a water phase outlet of the liquid-liquid separator is communicated with a first suction inlet of the jet mixer 4, and the liquid-liquid separator is also provided with an oil phase outlet.

Firstly, a certain amount of solid acid catalyst is pre-loaded in a reactor, deionized water is used as a continuous phase and is introduced into a system from a continuous phase inlet 3, mixed carbon four raw materials enter the bottom of a draft tube 6 in the reactor through a disperse phase inlet 1 and a disperse phase feeder 2, in order to achieve a good dispersing effect and ensure good circulation flow in the reactor, the pressure drop of the disperse phase feeder 2 is required to be 0.05-3.0 MPa, and the initial liquid flow rate at the outlet of the disperse phase feeder reaches 5-40 m/s. Inside the reactor, a heterogeneous contact reaction takes place. The reactant flows upwards in the draft tube 6, the apparent flow velocity is controlled to be larger than the critical settling velocity of the catalyst in the mixed liquid phase, the reactant flows upwards enter the expansion section 7 from the top of the draft tube 6 for primary settling separation, and most of the solid catalyst returns to the bottom of the straight tube section 5 of the reactor through the expansion section 7 and the down-flow area II of the straight tube section and contacts and reacts with fresh feed again. The reaction stream containing less catalyst particles at the top of the reactor enters the upper section 9 of the downcomer and enters the liquid-solid separator 10 for filtration separation. Reactant flow carries out cross flow filtration on the filtering component, and particles accumulated on the filtering pipe are washed by the reactant flow, so that the backwashing period of the filtering pipe is improved. Optionally, when the pressure difference between the two sides of the filter pipe is greater than 0.2MPa, the backwash liquid inlet 13 is introduced to backwash the filter pipe, so as to recover the permeability of the filter pipe. The backwash liquid is selected from the group consisting of a filtered supernatant or a fresh feed solution. The reactant flow after cross flow filtration is discharged out of the liquid-solid separator, enters the jet mixer 4 through the lower section 11 of the downcomer as a circulating material, is mixed with the materials from the continuous phase feed inlet 3 and the water phase outlet 17 in the liquid-liquid separator through the jet mixer 4, and then enters the bottom of the straight pipe section 5 of the reactor. Wherein the circulating mixed material is used as an intake fluid and the continuous liquid phase feed is used as a high velocity jet fluid. The filtered clear liquid enters the liquid-liquid separator 15 through the clear liquid outlet 12. The liquid-liquid separator 15 is used for separating oil phase and water phase, and can be a conventional gravity settling tank, an oil-water coalescence separator, a fiber membrane surface separator and a combination thereof. Wherein the separated oil phase is extracted through an oil phase outlet 16 and is further separated, and the separated water phase is returned to the bottom of the reactor 5 through a water phase outlet 17 for recycling.

The effect of the olefin hydration reaction method and system provided by the present invention is further illustrated by the following specific examples, but the present invention is not limited thereby.

Example 1

The examples illustrate the effectiveness of the olefin hydration reaction process provided by the present invention.

The reaction raw material is a mixed carbon four component containing isobutene, which is obtained from a catalytic cracking unit of a certain petroleum refinery in China petrochemical, and the composition of the reaction raw material is shown in Table 1. The solid acid catalyst is D005-II type resin produced by Dandong pearl Special resin Co Ltd, the particle size is 0.315-1.25 mm, and the wet density is 1.18-1.28 g/mL.

The flow of the olefin hydration process is shown in figure 1, wherein the diameter of the straight pipe section of the reactor is 48mm and the height is 1800 mm. A flow guide pipe with the diameter of 25.4mm is arranged in the reactor, and the area ratio of the ascending area to the descending area of the straight pipe section of the reactor is 0.39. The diameter of the expanded section of the reactor is 96mm, and the height of the expanded section is 400 mm.

Carbon four as a disperse phase enters the reactor from a disperse phase feeder, the disperse phase feeder is a 6mm sintered metal tube, the average pore diameter of the sintered metal tube is 7 mu m, and the pressure drop of the feeder is 0.25 MPa. Liquid-solid contact reaction is carried out in the reactor, wherein isobutene reacts with water under the action of a resin catalyst to generate tert-butyl alcohol. Reaction materials are extracted from the top of the reactor and enter a downcomer, the diameter of the downcomer is 48mm, a metal screen filtering component is arranged at the middle section of the downcomer, filtrate extracted by the filtering component enters a fiber membrane liquid separator for separating carbon four from water, and the structure of the fiber membrane separator is schematically shown in figure 2. The liquid-solid mixture on the interception side of the filtering component is used as circulating material, and is mixed with fresh water and water phase extracted from the bottom of the fiber membrane separator through a Venturi mixer (one of jet mixers) and then returns to the bottom of the reactor. The carbon four components extracted from the upper part of the fiber membrane separator tank are subjected to product separation to respectively obtain residual carbon four, tert-butyl alcohol and part of water.

The relative liquid hourly space velocity of the mixed carbon four raw material and the total amount of the catalyst in the reactor is 2.0h^-1The volume flow ratio of carbon four to water (the sum of fresh deionized water and circulating water) is 2:1, the reaction temperature is 60 ℃, and the pressure is 1.6 MPa.

The content of isobutene in the raw materials and the products is analyzed in a comparative manner by adopting an analysis method of ASTM D6733-01(2011), and the total conversion rate of isobutene is 73 percent by calculation.

Comparative example 1

Comparative example 1a conventional fixed bed reactor was used, the reactor diameter being 32mm and the height to diameter ratio being 12. The reaction raw materials and conditions of reaction temperature, pressure, space velocity, oil-water ratio, catalyst, etc. were the same as in example 1. The mixed C.sub.four feedstock and water are co-currently fed into the reactor. The top of the reactor was packed with a section of packing as initial distribution of material. After the reaction, the content change of isobutene in the raw materials and the product was analyzed, and the total conversion rate of isobutene was calculated to be 52%.

TABLE 1

Components	Mass fraction (%)
		Isobutane	9.0
N-butane	4.1
		1-butene	13.3
Isobutene	34.6
		Trans-2-butene	23.6
Cis-2-butene	15.3