Method and device for preparing tert-butyl alcohol by hydrating isobutene in raffinate C4

Abstract

The invention provides a method and a device for preparing tert-butyl alcohol by hydrating isobutene in raffinate C4, the raffinate C4 and water are used as raw materials and flow in a hydration reactor in a countercurrent manner, the isobutene in the raffinate C4 and the water react under the action of a catalyst to generate tert-butyl alcohol, the water and the tert-butyl alcohol are extracted from the bottom of the hydration reactor, and the tert-butyl alcohol is obtained. Liquid-phase residual C4 after reaction leaves the reactor from the upper part of the hydration reactor, and gas-phase C4 extracted from the top of the hydration reactor is condensed and gasified or compressed and then returns to the bottom of the reactor to serve as disturbance gas, so that the liquid-liquid-solid three-phase contact area is increased, the reaction rate is increased, and the reaction time is shortened; meanwhile, the generated tert-butyl alcohol product is timely removed from the reaction zone, so that the reaction is carried out in the positive direction, the conversion rate of isobutene is improved, and the method has higher economical efficiency by adopting a lower water-oil ratio and lower operation pressure.

Description

Technical Field

[0001] The invention relates to the technical field of petrochemical industry, in particular to a method and device for preparing tert-butyl alcohol by hydrating isobutylene in raffinate C4. Background Art

[0002] The boiling point difference between isobutylene and normal butene in the residual carbon four is very small. It is not economical to separate isobutylene from the residual carbon four by ordinary distillation. Generally, this part of carbon four is directly burned as fuel, which is a pity. Tert-butyl alcohol is an important organic chemical raw material and solvent, which is widely used in the fields of drug synthesis, coatings, dyes, fragrances and pesticides. In industry, tert-butyl alcohol is mainly obtained by the hydration reaction of isobutylene.

[0003] The hydration reaction of isobutylene to produce tert-butyl alcohol is an acid-catalyzed reaction. The existing tert-butyl alcohol production process mainly includes sulfuric acid hydration and ion exchange resin hydration. The sulfuric acid hydration method is relatively traditional. Its method is to use sulfuric acid to esterify isobutylene and then hydrolyze to produce tert-butyl alcohol. Its advantages are high conversion rate, but its disadvantages are long process, high energy consumption, serious equipment corrosion, and the production of a large amount of waste acid. Therefore, it has been gradually eliminated and replaced by the ion resin hydration method developed in the 1970s. Although the ion resin hydration method has a simpler process than the former, less three wastes are discharged, and there is basically no equipment corrosion problem, it generally has the technical problem of low isobutylene conversion rate. The main reason is that the oil-water two phases cannot achieve microscopic mixing in the ion exchange resin catalyst bed, and the contact between the two phases is insufficient.

[0004] Over the years, technicians have conducted a lot of research work on improving the isobutylene conversion rate and selectivity of ion resin hydration.

[0005] Patent CN1511814A discloses a method for preparing tert-butyl alcohol, which is to add a polyether nonionic surfactant with a viscosity average molecular weight of 200 to 800 during hydration. However, this nonionic surfactant "mixes" in water, and the use of a water circulation process will quickly block the catalyst pores and affect the service life of the catalyst. If water recycling is not implemented, water resources will be consumed greatly, and there is also a technical problem of difficulty in water purification.

[0006] Patent CN103804139A was searched and disclosed a method for preparing tert-butyl alcohol. The method uses multiple fixed bed reactors connected at the end, and tert-butyl alcohol aqueous solution is added to the first stage reactor, and the effective mass space velocity of the mixed carbon tetraisobutylene added to each subsequent stage reactor is equal. The method adds tert-butyl alcohol to the raw material, which increases the cost, and the process of controlling the mass of isobutylene added to each stage is complicated and cumbersome.

[0007] One of the existing isobutylene hydration methods is to use reactive extraction technology, in which water and C4 pass through the catalyst bed in a countercurrent manner, and water extracts tert-butyl alcohol in the reaction system, so that the isobutylene hydration proceeds in the positive direction to improve the conversion rate of isobutylene. The disadvantage of this method is that water as an extractant and reactant makes the water-to-oil ratio high, resulting in high energy consumption of the device and high operating pressure. Summary of the invention

[0008] In view of the shortcomings of the prior art, the present invention provides a method and device for preparing tert-butanol by hydrating isobutylene in residual carbon four, which can greatly improve the conversion rate of isobutylene hydration and use ion exchange resin as a catalyst to prepare tert-butanol by hydrating isobutylene.

[0009] To achieve the above object, the present invention is implemented by the following technical scheme: a method for preparing tert-butyl alcohol by hydrating isobutylene in residual carbon four, comprising the following steps:

[0010] S1: With raffinate C4 and water as raw materials, they flow countercurrently in a hydration reactor, and the isobutylene in the raffinate C4 and water react with the catalyst to generate tert-butyl alcohol;

[0011] S2: Water and tert-butyl alcohol are extracted from the bottom of the hydration reactor, and the residual C4 in the liquid phase after the reaction leaves the reactor from the top of the hydration reactor;

[0012] S3: The gaseous C4 extracted from the top of the hydration reactor is returned to the bottom of the reactor after condensation and gasification or compression, and serves as a disturbing gas, which increases the liquid-liquid-solid three-phase contact area and improves the reaction rate.

[0013] Preferably, the reaction temperature of the hydration reactor is 60-90°C, preferably 80-90°C, the reaction pressure is 0.6-1.50Mpa, preferably 0.9-1.2Mpa, the volume ratio of water to isobutylene in the raffinate C4 is 1-4, and the superficial flow velocity of the raffinate C4 is 0.1-1.0mm / s.

[0014] The device for preparing butanol by hydrating isobutylene in raffinate C4 of the present invention provides two processes, wherein the first process is for returning the circulating C4 to the bottom of the hydration reactor after condensation and gasification, and comprises a hydration reactor R, a liquid phase C4 tank V1, a condenser E1, a C4 circulation pump P1, a gasifier E2 and connecting pipelines between the devices. The hydration reactor is provided with a gas phase C4 outlet, a liquid phase C4 outlet, a water inlet, a raffinate C4 inlet, a gas phase C4 inlet and a tert-butyl alcohol water outlet in sequence from top to bottom. The gas phase C4 outlet at the top of the hydration reactor R is connected to the condenser E1, the condenser E1 outlet is connected to the liquid phase C4 tank V1, the liquid phase C4 outlet is connected to the C4 circulation pump P1, the C4 circulation pump P1 outlet is connected to the gas phase C4 inlet at the bottom of the hydration reactor through the gasifier E2, and is extracted as residual C4 all the way; the liquid phase C4 outlet at the top of the hydration reactor R is connected to the liquid phase C4 tank V1 through a pipeline.

[0015] The device for preparing tert-butyl alcohol by hydrating isobutylene in raffinate C4 of the present invention provides two processes. The second process is when the circulating C4 is compressed and returned to the bottom of the hydration reactor, the device includes a hydration reactor R, a liquid phase C4 tank V1, a C4 extraction pump P2, a C4 gas-liquid separation tank V2, a C4 compressor C1 and connecting pipelines between various devices. The hydration reactor is sequentially provided with a gas phase C4 outlet, a liquid phase C4 outlet, a water inlet, a raffinate C4 inlet, a gas phase C4 inlet and a tert-butyl alcohol water outlet from top to bottom. The gas phase C4 outlet at the top of the hydration reactor R is connected to the C4 gas-liquid separation tank V2, the liquid phase outlet of the C4 gas-liquid separation tank V2 is connected to the liquid phase C4 tank V1, the gas phase outlet of the C4 gas-liquid separation tank V2 is connected to the C4 compressor C1, and the outlet of the C4 compressor C1 is connected to the gas phase C4 inlet at the bottom of the hydration reactor; the liquid phase C4 outlet at the top of the hydration reactor R is connected to the liquid phase C4 tank V1 through a pipeline, the liquid phase C4 tank V1 is connected to the C4 production pump P2, and the C4 production pump P2 produces residual C4.

[0016] The hydration reactor used in the above two processes is the same.

[0017] The hydration reactor comprises a reaction section arranged between a water inlet and a raffinate C4 inlet, a top gas-liquid-liquid separation section between a water inlet and a gas-phase C4 inlet, and a bottom liquid-liquid stratification section below the raffinate C4 inlet. The reaction section is a multi-stage gas-lift loop reactor or a multi-stage fluidized bed structure, equipped with an ion exchange resin catalyst. The top gas-liquid-liquid separation section is provided with a gas-liquid separation and liquid-liquid stratification structure, such as a gas lift tray or a multi-stage sleeve. The multi-stage sleeve structure is composed of a plurality of concentric sleeves with a diameter greater than or equal to the reaction section shell, preferably 3 to 4 stages of concentric sleeves. The bottom liquid-liquid stratification section is equipped with fillers or is not provided with any internals.

[0018] The present invention provides a method and device for preparing tert-butyl alcohol by hydrating isobutylene in C4 residue. The method has the following beneficial effects:

[0019] 1. The present invention uses gaseous carbon four as a disturbance gas to increase the liquid-liquid-solid three-phase contact area and improve the reaction rate. At the same time, the generated tert-butyl alcohol product can be removed from the reaction zone in time, so that the reaction proceeds in the positive direction and the conversion rate of isobutylene is improved. The present invention uses a smaller water-oil ratio and a lower operating pressure, and has higher economy. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] Figure 1 It is a schematic diagram of the device process of the present invention;

[0021] Among them, R-hydration reactor; V1-liquid phase C4 tank; E1-condenser; P1-C4 circulation pump; E2-gasifier;

[0022] 1. Water inlet; 2. Extracted C4 inlet; 3. Gas phase C4 inlet; 4. Tert-butanol water outlet; 5. Gas phase C4 outlet; 6. Liquid phase C4 outlet; 7. Water pipeline; 8. Extracted C4 pipeline; 9. Residual C4 pipeline; 10. Tert-butanol water pipeline; 11. Gas phase C4 pipeline; 12. C4 condensate pipeline; 13. Liquid phase C4 pipeline; 14. Circulating liquid phase C4 pipeline; 15. Circulating gas phase C4 pipeline.

[0023] Figure 2 It is a schematic diagram of the second process of the device of the present invention.

[0024] Among them, R-hydration reactor; V1-liquid phase C4 tank; P2-C4 extraction pump; V2-C4 gas-liquid separation tank; C1-C4 compressor;

[0025] 1. Water inlet; 2. Extracted C4 inlet; 3. Gas-phase C4 inlet; 4. Tert-butanol water outlet; 5. Gas-phase C4 outlet; 6. Liquid-phase C4 outlet; 7. Water pipeline; 8. Extracted C4 pipeline; 9. Residual C4 pipeline; 10. Tert-butanol water pipeline; 11. Gas-phase C4 pipeline; 12. Liquid-phase C4 pipeline of gas-liquid separation tank; 13. Liquid-phase C4 pipeline; 14. Gas-phase C4 pipeline of gas-liquid separation tank; 15. Circulating gas-phase C4 pipeline. DETAILED DESCRIPTION

[0026] The technical solution of the present invention will be clearly and completely described below in conjunction with the accompanying drawings of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0027] Example:

[0028] Please refer to the attached Figure 1The gas phase C4 condensation and gasification process includes a hydration reactor R, a liquid phase C4 tank V1, a condenser E1, a C4 circulation pump P1, a gasifier E2 and connecting pipelines between the various devices. The hydration reactor R is provided with a gas phase C4 outlet 5, a liquid phase C4 outlet 6, a water inlet 1, a residual C4 inlet 2, a gas phase C4 inlet 3 and a tert-butyl alcohol water outlet 4 in sequence from top to bottom. The gas phase C4 outlet 5 at the top of the hydration reactor R is connected to the condenser E1 through a gas phase C4 pipeline 11, and the outlet of the condenser E1 is connected to the tert-butyl alcohol water outlet 4 through a gas phase C4 pipeline 12. The C4 condensate pipeline 11 is connected to the liquid C4 tank V1, and the outlet of the liquid C4 tank V1 is connected to the C4 circulation pump P1 through the circulating liquid C4 pipeline 14. The outlet of the C4 circulation pump P1 is connected to the gas phase C4 inlet 3 at the bottom of the hydration reactor R through the circulating gas phase C4 pipeline 15 after being gasified through the gasifier E2, and is also produced as residual C4 through the residual C4 pipeline 9; the liquid phase C4 outlet 6 at the upper part of the hydration reactor R is connected to the liquid phase C4 tank V1 through the liquid phase C4 pipeline 13.

[0029] Please refer to the attached Figure 2 The gas phase C4 compression process includes a hydration reactor R, a liquid phase C4 tank V1, a C4 extraction pump P2, a C4 gas-liquid separation tank V2, a C4 compressor C1 and connecting pipelines between the various devices. The hydration reactor R is provided with a gas phase C4 outlet 5, a liquid phase C4 outlet 6, a water inlet 1, a residual C4 inlet 2, a gas phase C4 inlet 3 and a tert-butyl alcohol water outlet 4 in sequence from top to bottom. The gas phase C4 outlet 5 at the top of the hydration reactor R is connected to the C4 gas-liquid separation tank V2 through a liquid phase C4 pipeline 13. The liquid phase outlet of the C4 gas-liquid separation tank V2 The inlet is connected to the liquid phase C4 tank V1 through the gas-liquid separation tank liquid phase C4 pipeline 12, the gas phase outlet of the C4 gas-liquid separation tank V2 is connected to the C4 compressor C1 through the gas-liquid separation tank gas phase C4 pipeline 14, and the outlet of the C4 compressor C1 is connected to the gas phase C4 inlet 3 at the bottom of the hydration reactor R through the circulating gas phase C4 pipeline 15; the liquid phase C4 6 outlet at the top of the hydration reactor R is connected to the liquid phase C4 tank V1 through a pipeline, the liquid phase C4 tank V1 is connected to the C4 production pump P2, and the C4 production pump P2 produces residual C4 through the residual C4 pipeline 9.

[0030] Attached Figure 1 and attached Figure 2 The hydration reactor used in both processes is the same.

[0031] The hydration reactor R comprises a reaction section arranged between a water inlet 1 and a raffinate C4 inlet 2, a top gas-liquid-liquid separation section between the water inlet 1 and a gas-phase C4 inlet 3, and a bottom liquid-liquid stratification section below the raffinate C4 inlet 2. The reaction section is a multi-stage gas-lift loop reactor or a multi-stage fluidized bed structure, equipped with an ion exchange resin catalyst, the top gas-liquid-liquid separation section is provided with a gas-liquid separation and liquid-liquid stratification structure, such as a gas lift plate or a multi-stage sleeve, etc. The multi-stage sleeve structure is composed of a plurality of concentric sleeves having a diameter larger than that of the reaction section shell, preferably 3 to 5 stages of concentric sleeves, and the bottom liquid-liquid stratification section is provided with fillers or is not provided with any internal parts.

[0032] The process principle of the present invention is that water and residual carbon four flow countercurrently into the reaction section of the hydration reactor, isobutylene in the residual carbon four reacts with water to generate tert-butanol under the action of a catalyst; water and tert-butanol are extracted from the bottom of the hydration reactor, and the liquid phase residual carbon four after the reaction leaves the reactor from the upper part of the hydration reactor; the gas phase carbon four extracted from the top of the hydration reactor is condensed and gasified or compressed and then returned to the bottom of the reactor as a disturbing gas, thereby increasing the liquid-liquid-solid three-phase contact area and improving the reaction rate.

[0033] Embodiment 1:

[0034] The reaction raw materials are raffinate C4 (mass composition is 1.96% isobutane, 7.50% normal butane, 0.06% isopentane, 0.07% normal pentane, 0.11% propylene, 10.35% trans-2-butene, 36.92% isobutylene, 33.91% normal butene, 9.11% cis-2-butene, 0.01% butadiene) and water, the volume ratio of water to isobutylene is 2:1, and they enter the reactor through the water inlet and the raffinate C4 inlet respectively. The apparent flow rate of the raffinate C4 is 0.5 mm / s. The reaction section of the hydration reactor adopts a fluidized bed structure and is equipped with an ion exchange resin catalyst. The reactor is operated at a pressure of 1.0 MPa and a temperature of 80-90°C. The isobutylene and water in the residual carbon four react to form tert-butyl alcohol under the action of the catalyst. The tert-butyl alcohol and water are extracted from the bottom of the reactor. The gas-liquid-liquid separation section at the top of the reactor is provided with a gas-lifting tray. The gas phase carbon four leaves the reactor from the gas lift pipe of the gas lift tray through the gas phase carbon four outlet. The liquid phase is a mixture of water and carbon four, which is layered on the gas lift tray. The upper layer is liquid phase carbon four and the lower layer is a water layer. The liquid phase carbon four is extracted from the liquid phase carbon four outlet to the liquid phase carbon four tank. The gas phase carbon four is condensed and gasified and then returned to the bottom of the reactor. After the above reaction process, the isobutylene conversion rate is 89%.

[0035] Embodiment 2:

[0036] The reaction raw materials are raffinate C4 (mass composition is 1.68% isobutane, 5.29% normal butane, 0.08% isopentane, 0.32% normal pentane, 0.23% propylene, 10.27% trans-2-butene, 38.35% isobutylene, 35.77% normal butene, 7.28% cis-2-butene, 0.73% butadiene) and water, the volume ratio of water to isobutylene is 4:1, and enter the reactor through the water inlet and the raffinate C4 inlet respectively. The apparent flow rate of the raffinate C4 is 0.6 mm / s. The reaction section of the hydration reactor adopts a fluidized bed structure and is equipped with an ion exchange resin The reactor is equipped with a lipid catalyst, and the operating pressure of the reactor is 1.2MPa, and the operating temperature is 82-93℃. The isobutylene and water in the residual carbon four react to form tert-butyl alcohol under the action of the catalyst. Tert-butyl alcohol and water are extracted from the bottom of the reactor. The gas-liquid-liquid separation section at the top of the reactor is provided with a 3-layer sleeve structure. The gas phase carbon four leaves the reactor from the inner sleeve through the gas phase carbon four outlet and returns after being compressed by the carbon four compressor. The liquid phase is a mixture of water and carbon four, which is layered between the second and third sleeve layers. The upper layer is liquid phase carbon four, and the lower layer is a water layer. The liquid phase carbon four is extracted from the liquid phase carbon four outlet to the liquid phase carbon four tank. After the above reaction process, the isobutylene conversion rate is 94.5%.

[0037] Embodiment 3:

[0038] The reaction raw materials are raffinate C4 (mass composition is 2.04% isobutane, 7.52% normal butane, 0.08% isopentane, 0.03% normal pentane, 0.12% propylene, 10.31% trans-2-butene, 36.73% isobutylene, 33.25% normal butene, 9.85% cis-2-butene, 0.07% butadiene) and water, the volume ratio of water to isobutylene is 3:1, and they enter the reactor through the water inlet and the raffinate C4 inlet respectively. The apparent flow rate of the raffinate C4 is 0.55 mm / s. The reaction section of the hydration reactor adopts a fluidized bed structure and is equipped with an ion exchange resin The reactor is equipped with a lipid catalyst, and the operating pressure is 0.9MPa and the operating temperature is 80-90℃. The isobutylene and water in the residual C4 react under the action of the catalyst to generate tert-butyl alcohol. Tert-butyl alcohol and water are extracted from the bottom of the reactor. The gas-liquid-liquid separation section at the top of the reactor is equipped with a 4-layer sleeve structure. The gas phase C4 leaves the reactor from the inner sleeve through the gas phase C4 outlet and returns after being compressed by the C4 compressor. The liquid phase is a mixture of water and C4, which is layered between the 2nd, 3rd and 4th sleeve layers. The upper layer is liquid phase C4, and the lower layer is a water layer. The liquid phase C4 is extracted from the liquid phase C4 outlet to the liquid phase C4 tank. After the above reaction process, the isobutylene conversion rate is 92.8%

[0039] Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that various changes, modifications, substitutions and variations may be made to the embodiments without departing from the principles and spirit of the present invention, and that the scope of the present invention is defined by the appended claims and their equivalents.

Claims

1. A method for preparing tert-butyl alcohol by hydrating isobutylene in raffinate C4, characterized in that: The following steps are involved: S1: With raffinate C4 and water as raw materials, they flow countercurrently in a hydration reactor, and the isobutylene in the raffinate C4 and water react with the catalyst to generate tert-butyl alcohol; S2: Water and tert-butyl alcohol are extracted from the bottom of the hydration reactor, and the residual C4 in the liquid phase after the reaction leaves the reactor from the top of the hydration reactor; S3: The gaseous C4 extracted from the top of the hydration reactor is returned to the bottom of the reactor after condensation and gasification or compression, and serves as a disturbing gas, which increases the liquid-liquid-solid three-phase contact area and improves the reaction rate.

2. The method for preparing tert-butyl alcohol by hydrating isobutylene in raffinate C4 according to claim 1, characterized in that: The reaction temperature of the hydration reactor is 60-90° C., preferably 80-90° C., the reaction pressure is 0.6-1.50 MPa, preferably 0.9-1.2 MPa, the volume ratio of water to isobutylene in the raffinate C4 is 1-4, and the superficial flow rate of the raffinate C4 is 0.1-1.0 mm / s.

3. The method for preparing tert-butyl alcohol by hydrating isobutylene in raffinate C4 according to claim 1, characterized in that: The hydration reactor comprises a reaction section arranged between a water inlet and a raffinate C4 inlet, a top gas-liquid-liquid separation section between the water inlet and the gas phase C4 inlet, and a bottom liquid-liquid stratification section below the raffinate C4 inlet.

4. The method for preparing tert-butyl alcohol by hydrating isobutylene in raffinate C4 according to claim 1, characterized in that: The reaction section is a multi-stage airlift loop reactor or a multi-stage fluidized bed structure, which is equipped with an ion exchange resin catalyst.

5. The method for preparing tert-butyl alcohol by hydrating isobutylene in raffinate C4 according to claim 1, characterized in that: The top gas-liquid-liquid separation section is provided with a gas-liquid separation and liquid-liquid stratification structure, and the liquid-liquid stratification structure is a multi-stage sleeve.

6. The method for preparing tert-butyl alcohol by hydrating isobutylene in raffinate C4 according to claim 5, characterized in that: The multi-stage sleeve structure is composed of a plurality of concentric sleeves with a diameter greater than or equal to the reaction section shell, preferably 3 to 4 stages of concentric sleeves, and the bottom liquid-liquid layering section is filled with fillers or is not provided with any internal parts.

7. A device for preparing tert-butyl alcohol by hydrating isobutylene in raffinate C4, comprising a hydration reactor R, a liquid phase C4 tank V1, a condenser E1, a C4 circulation pump P1, a gasifier E2 and connecting pipelines between the various devices, characterized in that: The circulating C4 is condensed and gasified and returns to the bottom of the hydration reactor. The hydration reactor is provided with a gas phase C4 outlet, a liquid phase C4 outlet, a water inlet, a residual C4 inlet, a gas phase C4 inlet and a tert-butanol water outlet in sequence from top to bottom. The gas phase C4 outlet at the top of the hydration reactor R is connected to the condenser E1, the condenser E1 outlet is connected to the liquid phase C4 tank V1, the liquid phase C4 outlet is connected to the C4 circulation pump P1, the C4 circulation pump P1 outlet is connected to the gas phase C4 inlet at the bottom of the hydration reactor through the gasifier E2, and is produced as residual C4; the liquid phase C4 outlet at the top of the hydration reactor R is connected to the liquid phase C4 tank V1 through a pipeline.

8. The device for preparing tert-butyl alcohol by hydrating isobutylene in raffinate C4 according to claim 7, characterized in that: When the circulating C4 is compressed and returned to the bottom of the hydration reactor, it includes a hydration reactor R, a liquid phase C4 tank V1, a C4 extraction pump P2, a C4 gas-liquid separation tank V2, a C4 compressor C1 and connecting pipelines between the various devices. The hydration reactor is provided with a gas phase C4 outlet, a liquid phase C4 outlet, a water inlet, a residual C4 inlet, a gas phase C4 inlet and a tert-butyl alcohol water outlet in sequence from top to bottom. The gas phase C4 outlet at the top of the hydration reactor R is connected to the C4 gas-liquid separation tank V2, the liquid phase outlet of the C4 gas-liquid separation tank V2 is connected to the liquid phase C4 tank V1, the gas phase outlet of the C4 gas-liquid separation tank V2 is connected to the C4 compressor C1, and the outlet of the C4 compressor C1 is connected to the gas phase C4 inlet at the bottom of the hydration reactor; the liquid phase C4 outlet at the top of the hydration reactor R is connected to the liquid phase C4 tank V1 through a pipeline, the liquid phase C4 tank V1 is connected to the C4 extraction pump P2, and the C4 extraction pump P2 extracts residual C4.

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