Superposition etherification co-production device

Abstract

The utility model discloses a superimposed etherification co-production device and a co-production method. The device comprises a superimposed etherification reactor, a catalytic distillation tower, a methanol extraction tower, a methanol recovery tower, an MTBE (Methyl Tert-Butyl Ether) product tower and a superimposed oil product tower, wherein the superimposed etherification reactor is connected with the catalytic distillation tower; the top of the catalytic distillation tower is connected with the methanol extraction tower; the methanol extraction tower is circularly connected with the methanol recovery tower; a tower kettle of the catalytic distillation tower is sequentially connected with the MTBE product tower and the superimposed oil product tower; and the methanol recovery tower is also connected with the superimposed etherification reactor. The utility model provides a full-flow process for producing superimposed oil and methyl tert-butyl ether from mixed C4, so that the superimposed oil and the methyl tert-butyl ether are produced after the mixed C4 is subjected to the processes of superimposed etherification, catalytic distillation, methanol recovery, rectification separation and the like, and the mixed C4 can be continuously used as a raw material of a subsequent device after isobutene is completely converted.

Description

Technical Field

[0001] The utility model relates to the technical field of petrochemical industry, and more specifically to a superimposed etherification co-production device. Background Art

[0002] As the gasoline specifications in the world continue to improve, the demand for high-octane components has increased dramatically. Catalytic cracking and steam cracking C4 fractions are currently important resources for producing high-octane gasoline components. Methyl tert-butyl ether (MTBE) can be obtained by etherification of isobutylene and methanol, which is an important anti-knock agent for the preparation of new formula gasoline. Dimerization of C4 olefins and subsequent hydrogenation can obtain multi-branched alkanes mainly composed of isooctane, whose composition is similar to that of isobutane-butene alkylation products, and is also an ideal clean gasoline blending component. At the same time, diisobutylene can also be used as a raw material for fine chemicals with good economic benefits. In the prior art, etherification and superposition reactions are generally carried out separately. The Petrochemical Research Institute has recently developed a new integrated superposition-etherification process that can produce MTBE and superposition products at the same time, and the ratio of MTBE to superposition products can be adjusted according to market needs. However, the isobutylene conversion rate of the prior art is only 80%-85%, and the remaining C4 after the reaction cannot be completely reacted because of isobutylene, resulting in the subsequent harsh process for the remaining isobutylene cannot be used. If the remaining C4 is used in the alkylation unit, it will lead to increased acid consumption and poor economic benefits. If the remaining C4 is used in the 1-butene unit, 1-butene products cannot be produced. Utility Model Content

[0003] In view of this, the purpose of the utility model is to avoid the shortcomings of the prior art, to simultaneously produce superimposed oil and methyl tert-butyl ether products from mixed C4 raw materials, to overcome the problems of low isobutylene conversion rate and high residual C4 isobutylene content in the production affecting subsequent use.

[0004] In order to achieve the above purpose, the utility model adopts the following technical solutions:

[0005] A superimposed etherification co-production device, comprising: a superimposed etherification reactor, a catalytic distillation tower, a methanol extraction tower, a methanol recovery tower, an MTBE product tower and a superimposed oil product tower;

[0006] Wherein, the stacked etherification reactor is connected to the catalytic distillation tower;

[0007] The top of the catalytic distillation tower is connected to the methanol extraction tower; the methanol extraction tower is cyclically connected to the methanol recovery tower;

[0008] The kettle of the catalytic distillation tower is connected to the MTBE product tower and the superimposed oil product tower in sequence;

[0009] The methanol recovery tower is also connected to the stacked etherification reactor.

[0010] Preferably, the above-mentioned superimposed etherification co-production device further comprises:

[0011] mixer;

[0012] The methanol recovery tower is connected to the superimposed etherification reactor through the mixer.

[0013] Preferably, the catalytic distillation tower is provided with a condenser 1 and a reboiler 1, and the catalytic distillation tower is connected to the methanol extraction tower through the condenser 1, and is connected to the MTBE product tower through the reboiler 1;

[0014] The methanol recovery tower is arranged between the second condenser and the second reboiler, the methanol recovery tower is connected to the mixer through the second condenser, and is connected to the methanol extraction tower through the second reboiler;

[0015] The MTBE product tower is provided with a condenser three and a reboiler three, and the MTBE product tower is connected to the superimposed oil product tower through the reboiler three;

[0016] The stacked oil product tower is provided with a condenser four and a reboiler four.

[0017] It can be seen from the above technical solution that compared with the prior art, the utility model has the following beneficial effects:

[0018] The utility model can expand the application scope of C4 after the mixed C4 is superposed and etherified, and aims at the process of producing superposed oil and methyl tert-butyl ether from mixed C4 raw materials, overcomes the problem that the isobutylene conversion rate is not high and the high isobutylene content of the produced residual C4 affects the subsequent use, and provides a connection method for the process of producing superposed oil and methyl tert-butyl ether from mixed C4. The superposed etherification reactor is used to carry out etherification and superposition reaction in the reactor, and then methanol is supplemented by catalytic distillation to make the isobutylene react completely, and then the methanol recovery system is used to complete the recycling of methanol, and the discharge of the catalytic distillation tower kettle enters the separation system to obtain methyl tert-butyl and superposed oil products. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] In order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings in the following description are only embodiments of the utility model. For ordinary technicians in this field, other drawings can be obtained based on the provided drawings without paying creative work.

[0020] Figure 1 This is the structural diagram of the superimposed etherification co-production device of the utility model;

[0021] Among them, in the figure:

[0022] 1-superimposed etherification reactor; 2-catalytic distillation tower; 3-methanol extraction tower; 4-methanol recovery tower; 5-MTBE product tower; 6-superimposed oil product tower; 7-mixer; 8-condenser one; 9-reboiler one; 10-condenser two; 11-reboiler two; 12-condenser three; 13-reboiler three; 14-condenser four; 15-reboiler four. DETAILED DESCRIPTION

[0023] The following will be combined with the drawings in the embodiments of the utility model to clearly and completely describe the technical solutions in the embodiments of the utility model. Obviously, the described embodiments are only part of the embodiments of the utility model, not all of the embodiments. Based on the embodiments in the utility model, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the utility model.

[0024] Example 1

[0025] See also Figure 1 This embodiment provides a superimposed etherification co-production device, including: a superimposed etherification reactor 1, a catalytic distillation tower 2, a methanol extraction tower 3, a methanol recovery tower 4, an MTBE product tower 5, a superimposed oil product tower 6 and a mixer 7;

[0026] Wherein, the stacked etherification reactor 1 is connected to the catalytic distillation tower 2;

[0027] The top of the catalytic distillation tower 2 is connected to the methanol extraction tower 3; the methanol extraction tower 3 is cyclically connected to the methanol recovery tower 4;

[0028] The bottom of the catalytic distillation tower 2 is connected to the MTBE product tower 5 and the superimposed oil product tower 6 in sequence;

[0029] The methanol recovery tower 4 is connected to the stacked etherification reactor 1 via a mixer 7 .

[0030] In this embodiment, the catalytic distillation tower 2 is provided with a condenser 8 and a reboiler 9, and the catalytic distillation tower 2 is connected to the methanol extraction tower 3 through the condenser 8, and is connected to the MTBE product tower 5 through the reboiler 9;

[0031] The methanol recovery tower 4 is disposed between the condenser 10 and the reboiler 11. The methanol recovery tower 4 is connected to the mixer 7 through the condenser 10 and is connected to the methanol extraction tower 3 through the reboiler 11.

[0032] The MTBE product tower 5 is provided with a condenser three 12 and a reboiler three 13, and the MTBE product tower 5 is connected to the superimposed oil product tower 6 via the reboiler three 13;

[0033] The stacked oil product tower 6 is provided with a condenser four 14 and a reboiler four 15.

[0034] Example 2

[0035] The method for using the superimposed etherification co-production device in Example 1 comprises the following steps:

[0036] (1) Mixed C4, methanol and methanol recovered from a methanol recovery tower are fed into a mixer 7 for mixing and then fed into a superimposed etherification reactor 1; in the superimposed etherification reactor 1, isobutylene reacts with methanol to generate MTBE, and olefins react with olefins to generate superimposed oil, and the discharged material enters the lower part of the reaction section of a catalytic distillation tower 2;

[0037] (2) Methanol is added from the top, middle and bottom of the catalytic distillation tower 2. Methanol and unreacted isobutylene continue to react in the reaction section of the catalytic distillation tower 2. After separation, the C4 containing methanol at the top of the tower enters the lower part of the methanol extraction tower 3 and is extracted in the methanol extraction tower 3;

[0038] (3) C4 without methanol is discharged from the top of the methanol extraction tower 3, and the water containing methanol in the methanol extraction tower 3 enters the methanol recovery tower 4, where the methanol and the extracted water are separated;

[0039] (4) The recovered methanol at the top of the methanol recovery tower 4 is returned to the mixer 7, and the extracted water at the bottom of the tower is returned to the methanol extraction tower 3;

[0040] (5) The discharge from the bottom of the catalytic distillation tower 2 enters the MTBE recovery tower 5, and the MTBE product is obtained at the top of the MTBE recovery tower 5. The discharge from the bottom of the MTBE recovery tower 5 enters the superimposed oil product tower 6, and the superimposed oil product is obtained at the top of the superimposed oil product tower 6. The heavy components are obtained in the bottom of the superimposed oil product tower 6.

[0041] The parameters involved in the above method are as follows:

[0042] The mass content of isobutylene in the raw material mixed carbon four is 6% to 20%.

[0043] Superimposed etherification reactor 1: temperature 40-70°C, pressure 0.6MPa-1.2MPa, space velocity 1-4h -1 , the alcohol-olefin ratio is 0.4 to 0.8:1.

[0044] Catalytic distillation tower 2: tower top temperature 40-60°C, tower top pressure 0.4MPa-0.6MPa, reflux ratio 0.5-3.0:1, molar ratio of supplementary methanol to isobutylene at the outlet of the superimposed etherification reactor is 3-5:1.

[0045] Methanol extraction tower 3: temperature 30-40°C, pressure 0.4MPa-0.8MPa, weight ratio of water to C4 0.1-0.2:1.

[0046] Methanol recovery tower 4: tower top temperature 65-90°C, tower top pressure 0-0.3MPa, reflux ratio 5-15:1.

[0047] MTBE product tower 5: top temperature 55-70°C, top pressure 0-0.3MPa, reflux ratio 0.3-3:1.

[0048] Superimposed oil product tower 6: tower top temperature 60~102℃, tower top pressure -0.6MPa~0MPa, reflux ratio 0.3~3:1.

[0049] The isobutylene content in the remaining C4 obtained is less than 0.1%, the purity of the MTBE product is ≥96%, and the purity of the superimposed oil product is ≥98%.

[0050] In this specification, each embodiment is described in a progressive manner, and each embodiment focuses on the differences from other embodiments. The same or similar parts between the embodiments can be referred to each other. For the device disclosed in the embodiment, since it corresponds to the method disclosed in the embodiment, the description is relatively simple, and the relevant parts can be referred to the method part.

[0051] The above description of the disclosed embodiments enables those skilled in the art to implement or use the present invention. Various modifications to these embodiments will be apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the present invention. Therefore, the present invention will not be limited to the embodiments shown herein, but will conform to the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A superimposed etherification co-production device, characterized in that: include: Superimposed etherification reactor, catalytic distillation tower, methanol extraction tower, methanol recovery tower, MTBE product tower and superimposed oil product tower; Wherein, the stacked etherification reactor is connected to the catalytic distillation tower; The top of the catalytic distillation tower is connected to the methanol extraction tower; the methanol extraction tower is cyclically connected to the methanol recovery tower; The kettle of the catalytic distillation tower is connected to the MTBE product tower and the superimposed oil product tower in sequence; The methanol recovery tower is also connected to the stacked etherification reactor.

2. A superimposed etherification co-production device according to claim 1, characterized in that: Also includes: mixer; The methanol recovery tower is connected to the superimposed etherification reactor through the mixer.

3. A superimposed etherification co-production device according to claim 2, characterized in that: The catalytic distillation tower is provided with a condenser 1 and a reboiler 1, the catalytic distillation tower is connected to the methanol extraction tower through the condenser 1, and is connected to the MTBE product tower through the reboiler 1; The methanol recovery tower is arranged between the second condenser and the second reboiler, the methanol recovery tower is connected to the mixer through the second condenser, and is connected to the methanol extraction tower through the second reboiler; The MTBE product tower is provided with a condenser three and a reboiler three, and the MTBE product tower is connected to the superimposed oil product tower through the reboiler three; The stacked oil product tower is provided with a condenser four and a reboiler four.

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