Device for producing isobutene by cracking methyl tert-butyl ether

Abstract

The utility model belongs to the technical field of methyl tert-butyl ether cracking, and particularly relates to a device for producing isobutene by cracking methyl tert-butyl ether. The device for producing isobutene by cracking methyl tert-butyl ether comprises an MTBE refining tower, the MTBE refining tower is connected with a cracking reactor, the bottom of the cracking reactor is sequentially connected with a condensate water cooler and a circulating water cooler, the circulating water cooler is connected with an absorption cooling tower, the absorption cooling tower is connected with a compressor inlet buffer tank, and the compressor inlet buffer tank is connected with a compressor outlet buffer tank. The compressor inlet buffer tank is connected with the gas production compressor; and the gas production compressor is connected with the isobutene water washing tower. According to the device for producing isobutene by cracking methyl tert-butyl ether, the condensate water cooler and the circulating water cooler are arranged and are matched with the light component removal tower reboiler, so that the cyclic utilization of heat is realized, and the energy consumption of the device is reduced; meanwhile, the isobutene water washing tower and the methanol water collecting tank are arranged, so that the loss of methanol is reduced, and the purity of an isobutene product is improved.

Description

Technical Field

[0001] This utility model belongs to the field of methyl tert-butyl ether cracking technology, specifically relating to a device for producing isobutylene by cracking methyl tert-butyl ether. Background Technology

[0002] Isobutylene is a colorless, flammable gas with an unpleasant odor at room temperature and atmospheric pressure. It is an important chemical raw material used in the production of polyisobutylene rubber, butyl rubber, isoprene, and other processed products. It is also a crucial raw material for the production of methyl methacrylate, which can be further processed into acrylic glass. In addition, isobutylene is widely used as a raw material in pharmaceuticals, pesticides, antioxidants, synthetic high-grade lubricants, gasoline additives, and other fine chemical products.

[0003] The main industrial production methods for isobutylene include sulfuric acid absorption, resin hydration dehydration, and methyl tert-butyl ether (MTBE) cracking. The sulfuric acid absorption method suffers from poor reaction selectivity, severe equipment corrosion, and difficulty in recovering and treating waste acid. The main drawback of the resin dehydration method is the low single-pass conversion rate of isobutylene in the C4 fraction (which increases the difficulty of further 1-butene extraction). Multi-stage hydration can improve the conversion rate, but it consumes more energy. The MTBE cracking method produces isobutylene with high yield and selectivity, a simple process, and low investment costs, making it suitable for large-scale production. However, existing MTBE cracking technologies produce isobutylene with a purity of only 99.5%, which does not meet the 99.9% polymerization requirement, and their high energy consumption hinders the widespread adoption of MTBE cracking technology.

[0004] CN209065794U discloses an apparatus for producing high-purity isobutylene by MTBE cracking, including an MTBE light phase removal tower, a heavy phase removal tower, a cracking reactor, a gas-liquid separator, and newly added liquid phase water washing tower and methanol refining tower. It improves the purity of the product by recovering the waste heat of cracking and preheating the raw materials through dual heat exchangers, removing impurities from the gas phase isobutylene through deep water washing, and refining and purifying the liquid phase methanol. At the same time, it reduces energy consumption through waste heat recovery. However, it only focuses on the preheating of the cracking stage and does not integrate it with the subsequent equipment. Moreover, the efficiency of the heat exchangers is limited by the cracking reaction temperature, and the waste heat recovery is poor under extreme conditions.

[0005] Therefore, it is particularly important to develop a simple and energy-efficient MTBE cracking device for isobutylene production. Utility Model Content

[0006] The purpose of this invention is to overcome the defects of the existing technology and provide a device for producing isobutylene by cracking methyl tert-butyl ether. After cracking methyl tert-butyl ether, a condensate cooler and a circulating water cooler are set up, which, together with the reboiler at the bottom of the light-weight removal tower, realizes the recycling of heat and reduces the energy consumption of the device. At the same time, an isobutylene washing tower and a methanol-water collection tank are set up to reduce methanol loss and improve the purity of the isobutylene product.

[0007] The methyl tert-butyl ether (MTBE) cracking to isobutylene apparatus of this invention includes an MTBE conveying pipeline connected to an MTBE refining tower for conveying MTBE feedstock; a pipeline connected to a cracking reactor is located in the middle of the MTBE refining tower; C5 fraction, as a light component, is collected from the top of the MTBE refining tower and conveyed via the C5 pipeline; heavy components are collected from the bottom of the MTBE refining tower and conveyed to subsequent equipment via a heavy component output pipeline; the bottom of the cracking reactor is sequentially connected to a condensate cooler and a circulating water cooler, and the circulating water... The cooler is connected to the absorption cooling tower. The top of the absorption cooling tower is equipped with a pipeline connected to the compressor inlet buffer tank. The compressor inlet buffer tank is connected to the gas-producing compressor. The gas-producing compressor is connected to the isobutylene washing tower. The top of the isobutylene washing tower is equipped with a pipeline connected to the isobutylene feed buffer tank. The isobutylene feed buffer tank is connected to the isobutylene light removal tower. The bottom of the isobutylene light removal tower is equipped with a pipeline connected to the isobutylene heavy removal tower. The top of the isobutylene heavy removal tower is connected to the isobutylene pipeline for conveying the generated isobutylene. The bottom of the isobutylene heavy removal tower is connected to the heavy C4 pipeline.

[0008] Preferably, the condensate cooler is provided with a refrigerant inlet, a refrigerant outlet, a heat medium inlet, and a heat medium outlet. The refrigerant in the condensate cooler is steam condensate, and the heat medium is the gas generated by the pyrolysis reactor. The gas generated by the pyrolysis reactor enters the condensate cooler through the heat medium inlet, and after cooling, it is connected to the circulating water cooler through the heat medium outlet. The refrigerant outlet of the condensate cooler is connected to the reboiler A of the light-light-removal tower, and the reboiler A of the light-light-removal tower is provided with a pipeline connected to the refrigerant inlet of the condensate cooler.

[0009] Preferably, the steam condensate is used as the heat medium for the light precipitator reboiler A after heat exchange in the condensate cooler. After heat exchange in the light precipitator reboiler A, it is circulated to the cold medium inlet of the condensate cooler as a cold medium. The cold medium for the light precipitator reboiler A is the bottom material of the isobutylene light precipitator.

[0010] Preferably, the upper part of the absorption cooling tower is connected to the extractant pipeline, the bottom of the absorption cooling tower is provided with a pipeline connected to the methanol recovery tower, the bottom of the methanol recovery tower is provided with a pipeline for reflux to the upper part of the absorption cooling tower, and the top of the methanol recovery tower is connected to the methanol refining tower.

[0011] Preferably, the top of the methanol refining tower is provided with a pipeline connected to the compressor inlet buffer tank, and the bottom is connected to a methanol pipeline.

[0012] Preferably, the upper part of the isobutylene washing tower is connected to the demineralized water pipeline, and the bottom part is connected to the sewage pipeline.

[0013] Preferably, the bottom of the isobutylene light-weight removal tower is provided with a light-weight removal tower reboiler A and a light-weight removal tower reboiler B, and the top is connected to the fuel gas pipeline; the light-weight removal tower reboiler B is provided with a heat medium inlet and a heat medium outlet, the heat medium inlet is connected to the low-pressure steam input pipeline, and the refrigerant of the light-weight removal tower reboiler B is the bottom material of the isobutylene light-weight removal tower; the low-pressure steam output pipeline is provided with a pipeline connected to the condensate cooler to replenish the condensate in time and ensure the heat exchange effect.

[0014] Preferably, the bottom of both the compressor inlet buffer tank and the isobutylene feed buffer tank is provided with a pipeline connected to the water collection tank, and the water collection tank is provided with a pipeline connected to the absorption cooling tower.

[0015] Specifically, the operation process of the methyl tert-butyl ether (MTBE) cracking to isobutylene unit is as follows: MTBE from outside the boundary enters the middle of the MTBE refining tower through the MTBE delivery pipeline. In the MTBE refining tower, light and heavy components are separated. The C5 component, as the light component, is drawn from the top of the MTBE refining tower, and the MSBE, as the heavy component, is drawn from the bottom of the tower. The refined MTBE is drawn from the gas phase in the middle of the tower and enters the cracking reactor. Inside the cracking reactor, MTBE undergoes a cracking reaction to generate isobutylene and methanol, accompanied by a small amount of side reactions. The gas generated by the cracking reaction is first cooled to 90°C by a condensate cooler, and then cooled to 40°C by a circulating water cooler.

[0016] The cooled pyrolysis products enter from the bottom of the absorption cooling tower, the extractant enters from the top of the absorption cooling tower, and the gaseous isobutylene is collected from the top of the absorption cooling tower. Most of the methanol is absorbed by the absorption cooling tower. The methanol-water mixture from the bottom of the absorption cooling tower enters the middle of the methanol recovery tower. The methanol and water are separated by the methanol recovery tower. The methanol from the top enters the methanol refining tower, and the water from the bottom is used as the extractant to enter the upper part of the absorption cooling tower for recycling.

[0017] Inside the methanol refining tower, crude methanol is purified, and a small amount of isobutylene is recovered. Light components such as isobutylene are taken out from the top of the tower and mixed with crude isobutylene from the top of the absorption cooling tower before entering the compressor inlet buffer tank. Refined methanol is taken out from the bottom of the methanol refining tower and transported to subsequent units via methanol pipeline.

[0018] Crude isobutylene undergoes sedimentation separation in the compressor inlet buffer tank, separating most of the water. The crude isobutylene after water separation enters the gas-generating compressor. The gaseous isobutylene is pressurized by the gas-generating compressor and becomes liquid, entering the lower part of the isobutylene water washing tower. Demineralized water from outside the boundary enters from the upper part of the isobutylene water washing tower. Isobutylene without methanol is collected from the top of the isobutylene water washing tower and then enters the isobutylene feed buffer tank for hydrocarbon-water separation, separating some water. The isobutylene after water separation enters the isobutylene light component removal tower, where light components such as dimethyl ether are separated. The light components are collected from the top of the isobutylene light component removal tower and sent out of the boundary as fuel gas.

[0019] Crude isobutylene, after the light components have been removed, is collected from the bottom of the isobutylene light component removal tower and enters the isobutylene heavy component removal tower. The product isobutylene is collected from the top of the isobutylene heavy component removal tower, while the heavy component C4 is collected from the bottom of the isobutylene heavy component removal tower.

[0020] Water separated from the compressor inlet buffer tank and the isobutylene feed buffer tank enters the water collection tank. The collected water is recycled and the isobutylene in it is recovered. The water is then returned to the bottom inlet of the absorption cooling tower, mixed with fresh pyrolysis products, and then enters the absorption cooling tower.

[0021] The condensate heated by the condensate cooler is used as a heat transfer medium in the reboiler A of the light-weight removal tower. The condensate cooled by the reboiler A is recycled and returned to the condensate cooler as a coolant. To avoid insufficient heat provided by the condensate, the isobutylene light-weight removal tower is also equipped with a reboiler B to provide the remaining heat to the isobutylene light-weight removal tower. The heat transfer medium of the reboiler B is low-pressure steam. At the same time, the condensate generated by the low-pressure steam heat exchange can be transported to the condensate cooler to supplement the condensate loss caused by heat exchange in the condensate cooler and the reboiler A of the light-weight removal tower, so as to ensure the heat exchange effect.

[0022] Compared with the prior art, the beneficial effects of this utility model are as follows:

[0023] (1) The methyl tert-butyl ether cracking to produce isobutylene device of this invention first cools the cracking product by steam condensate and then by circulating water. The heated steam condensate is used as a heat medium for the isobutylene light removal tower reboiler, which reduces the amount of circulating water and steam used.

[0024] (2) The methyl tert-butyl ether cracking to produce isobutylene device of this utility model is equipped with a methanol-water collection tank, which collects the water from the device and sends it to the absorption cooling tower to further recover the C4 and methanol components, while reducing wastewater discharge; secondly, an isobutylene water washing tower is set up to reduce the content of methanol and dimethyl ether in the product, improve the product purity, and improve the efficiency of the device. Attached Figure Description

[0025] Figure 1 This is a schematic diagram of the apparatus for producing isobutylene by cracking methyl tert-butyl ether in this invention.

[0026] In the diagram: 1. MTBE refining tower; 2. Cracking reactor; 3. Condensate cooler; 4. Circulating water cooler; 5. Absorption cooling tower; 6. Methanol recovery tower; 7. Methanol refining tower; 8. Compressor inlet buffer tank; 9. Gas-producing compressor; 10. Isobutylene washing tower; 11. Isobutylene feed buffer tank; 12. Isobutylene light component removal tower; 13. Light component removal tower reboiler A; 14. Light component removal tower reboiler B; 15. Isobutylene heavy component removal tower; 16. Water collection tank; 17. MTBE conveying pipeline; 18. C5 pipeline; 19. Heavy component output pipeline; 20. Methanol pipeline; 21. Wastewater pipeline; 22. Demineralized water pipeline; 23. Fuel gas pipeline; 24. Heavy C4 pipeline; 25. Isobutylene pipeline; 26. Low-pressure steam output pipeline; 27. Low-pressure steam input pipeline; 28. Extractant pipeline. Detailed Implementation

[0027] The technical solution of this utility model will be further described below with reference to the accompanying drawings.

[0028] like Figure 1 As shown, the methyl tert-butyl ether (MTBE) cracking unit for isobutylene production includes an MTBE refining tower 1. The MTBE refining tower 1 has a pipeline connected to a cracking reactor 2 in its middle section. The bottom of the cracking reactor 2 is sequentially connected to a condensate cooler 3 and a circulating water cooler 4. The circulating water cooler 4 is connected to an absorption cooling tower 5. The top of the absorption cooling tower 5 has a pipeline connected to a compressor inlet buffer tank 8. The compressor inlet buffer tank 8 is connected to a gas-producing compressor 9. The gas-producing compressor 9 is connected to an isobutylene washing tower 10. The top of the isobutylene washing tower 10 has a pipeline connected to an isobutylene feed buffer tank 11. The isobutylene feed buffer tank 11 is connected to an isobutylene light-weight removal tower 12. The bottom of the isobutylene light-weight removal tower 12 has a pipeline connected to an isobutylene heavy-weight removal tower 15. The top of the isobutylene heavy-weight removal tower 15 is connected to an isobutylene pipeline 25 for conveying the generated isobutylene. The bottom of the isobutylene heavy-weight removal tower 15 is connected to a heavy C4 pipeline 24.

[0029] The MTBE refining tower 1 is connected to the MTBE conveying pipeline 17. The light component of the MTBE refining tower 1 is extracted from the top of the tower and conveyed through the C5 pipeline 18. The heavy component of the MTBE refining tower 1 is conveyed to the downstream equipment through the heavy component output pipeline 19 at the bottom of the tower.

[0030] The condensate cooler 3 is provided with a refrigerant inlet, a refrigerant outlet, a heat medium inlet, and a heat medium outlet. The refrigerant in the condensate cooler 3 is steam condensate, and the heat medium is the gas generated by the cracking reactor 2. The gas generated by the cracking reactor 2 enters the condensate cooler 3 through the heat medium inlet, and after cooling, it is connected to the circulating water cooler 4 through the heat medium outlet. The refrigerant outlet of the condensate cooler 3 is connected to the light-light tower reboiler A13, and the light-light tower reboiler A13 is provided with a pipeline connected to the refrigerant inlet of the condensate cooler 3.

[0031] The steam condensate is used as the heat medium for the light precipitator reboiler A13 after heat exchange in the condensate cooler 3. After heat exchange in the light precipitator reboiler A13, it is circulated to the cold medium inlet of the condensate cooler 3 as a cold medium. The cold medium of the light precipitator reboiler A13 is the bottom material of the isobutylene light precipitator 12.

[0032] The upper part of the absorption cooling tower 5 is connected to the extractant pipeline 28, the bottom of the absorption cooling tower 5 is provided with a pipeline connected to the methanol recovery tower 6, the bottom of the methanol recovery tower 6 is provided with a pipeline for reflux to the upper part of the absorption cooling tower 5, and the top of the methanol recovery tower 6 is connected to the methanol refining tower 7.

[0033] The top of the methanol refining tower 7 is connected to the compressor inlet buffer tank 8, and the bottom is connected to the methanol pipeline 20.

[0034] The upper part of the isobutylene washing tower 10 is connected to the demineralized water pipeline 22, and the bottom part is connected to the sewage pipeline 21.

[0035] The bottom of the isobutylene light-removal tower 12 is equipped with a light-removal tower reboiler A13 and a light-removal tower reboiler B14, and the top is connected to the fuel gas pipeline 23. The light-removal tower reboiler B14 is equipped with a heat medium inlet and a heat medium outlet. The heat medium inlet is connected to the low-pressure steam input pipeline 27, and the refrigerant of the light-removal tower reboiler B14 is the bottom material of the isobutylene light-removal tower 12. The low-pressure steam output pipeline 26 is equipped with a pipeline connected to the condensate cooler 3.

[0036] The compressor inlet buffer tank 8 and the isobutylene feed buffer tank 11 are both equipped with pipelines at the bottom that connect to the water collection tank 16, and the water collection tank 16 is equipped with pipelines that connect to the absorption cooling tower 5.

[0037] Specifically, the operation process of the methyl tert-butyl ether cracking to produce isobutylene is as follows: MTBE from outside the boundary enters the middle of MTBE refining tower 1 through MTBE conveying pipeline 17. In MTBE refining tower 1, light and heavy components are separated. The C5 component, as the light component, is taken out from the top of MTBE refining tower 1 through C5 pipeline 18, and MSBE, as the heavy component, is taken out from the bottom of the tower through heavy component output pipeline 19. The refined MTBE is taken out from the middle of the tower in the gas phase and enters cracking reactor 2. Inside cracking reactor 2, MTBE undergoes cracking reaction to generate isobutylene and methanol, accompanied by a small amount of side reaction. The gas generated by the cracking reaction is first cooled to 90°C by condensate cooler 3, and then cooled to 40°C by circulating water cooler 4.

[0038] The cooled pyrolysis products enter from the lower part of the absorption cooling tower 5, and the extractant enters from the upper part of the absorption cooling tower 5 through the extractant pipeline 28. The gaseous isobutylene is collected from the top of the absorption cooling tower 5 and absorbs most of the methanol. The methanol-water mixture from the bottom of the absorption cooling tower 5 enters the middle part of the methanol recovery tower 6. The methanol and water are separated by the methanol recovery tower 6. The methanol from the top enters the methanol refining tower 7, and the water from the bottom is recycled as an extractant in the upper part of the absorption cooling tower 5.

[0039] Crude methanol is purified inside methanol refining tower 7, and a small amount of isobutylene is recovered. Light components such as isobutylene are taken out from the top of the tower and mixed with crude isobutylene from the top of absorption cooling tower 5 before entering compressor inlet buffer tank 8. Refined methanol is taken out from the bottom of methanol refining tower 7 and transported to downstream units via methanol pipeline 20. Crude isobutylene undergoes sedimentation separation in the compressor inlet buffer tank 8, separating most of the water. The crude isobutylene after water separation enters the gas-generating compressor 9. After being pressurized by the gas-generating compressor 9, the gaseous isobutylene becomes liquid and enters the lower part of the isobutylene water washing tower 10. Demineralized water from outside the boundary enters from the upper part of the isobutylene water washing tower 10 through the demineralized water pipeline 22. Isobutylene without methanol is collected from the top of the isobutylene water washing tower 10 and then enters the isobutylene feed buffer tank 11 for hydrocarbon-water separation, separating some water. The isobutylene after water separation enters the isobutylene light component removal tower 12. Light components such as dimethyl ether are separated in the isobutylene light component removal tower 12. The light components are collected from the top of the isobutylene light component removal tower 12 through the fuel gas pipeline 23 and sent out of the boundary as fuel gas.

[0040] Crude isobutylene, from which light components have been removed, is collected from the bottom of isobutylene light component removal tower 12 and enters isobutylene heavy component removal tower 15. Product isobutylene is collected from the top of isobutylene heavy component removal tower 15 through isobutylene pipeline 25, and heavy component C4 is collected from the bottom of isobutylene heavy component removal tower 15 through heavy C4 pipeline 24.

[0041] Water separated from the compressor inlet buffer tank 8 and the isobutylene feed buffer tank 11 enters the water collection tank 16. The collected water is recycled and the isobutylene in it is recovered. The water is then returned to the bottom inlet of the absorption cooling tower 5 and mixed with the fresh cracking products before entering the absorption cooling tower 5.

[0042] The condensate heated by the condensate cooler 3 is used as a heat transfer medium in the reboiler A13 of the light-weight removal tower. The condensate cooled by the reboiler A13 is recycled and returned to the condensate cooler 3 as a coolant. To avoid insufficient heat provided by the condensate, the isobutylene light-weight removal tower 12 is also equipped with a reboiler B14 to provide the remaining heat to the isobutylene light-weight removal tower 12. The heat transfer medium of the reboiler B14 is the low-pressure steam inlet pipe 27. At the same time, the condensate generated by the heat exchange in the low-pressure steam inlet pipe 27 can be transported to the condensate cooler 3 through the low-pressure steam outlet pipe 26 to supplement the condensate loss caused by heat exchange in the condensate cooler 3 and the reboiler A13 of the light-weight removal tower, thus ensuring the heat exchange effect.

Claims

1. A plant for the production of isobutene by cracking methyl tert-butyl ether, characterized in that, The application relates to a production system of isobutene, which comprises an MTBE refining tower (1), a cracking reactor (2), an absorption cooling tower (5), an isobutene water washing tower (10), an isobutene light component removal tower (12) and an isobutene heavy component removal tower (15), wherein a pipeline is arranged in the middle of the MTBE refining tower (1) and connected with the cracking reactor (2); the bottom of the cracking reactor (2) is sequentially connected with a condensate cooler (3) and a circulating water cooler (4); the circulating water cooler (4) is connected with the absorption cooling tower (5); the top of the absorption cooling tower (5) is provided with a pipeline connected with a compressor inlet buffer tank (8); the compressor inlet buffer tank (8) is connected with a gas production compressor (9); the gas production compressor (9) is connected with the isobutene water washing tower (10); the top of the isobutene water washing tower (10) is provided with a pipeline connected with an isobutene feeding buffer tank (11); the isobutene feeding buffer tank (11) is connected with the isobutene light component removal tower (12); the bottom of the isobutene light component removal tower (12) is provided with a pipeline connected with the isobutene heavy component removal tower (15); and the top of the isobutene heavy component removal tower (15) is connected with an isobutene pipeline (25) for conveying generated isobutene.

2. The apparatus for the production of isobutene by cleavage of methyl tert-butyl ether according to claim 1, characterized in that The MTBE refining tower (1) is connected with an MTBE conveying pipeline (17); light components of the MTBE refining tower (1) are taken out from the top and conveyed through a C5 pipeline (18); and heavy components of the MTBE refining tower (1) are conveyed to subsequent devices through a heavy component output pipeline (19) at the bottom.

3. The apparatus for the production of isobutylene by the cleavage of methyl tert-butyl ether according to claim 1, characterized in that, The bottom of the isobutene light component removal tower (12) is provided with a light component removal tower reboiler A (13) and a light component removal tower reboiler B (14), and the top is connected with a fuel gas pipeline (23); the light component removal tower reboiler B (14) is provided with a heat medium inlet and a heat medium outlet; the heat medium inlet is connected with a low-pressure steam input pipeline (27); the heat medium outlet is connected with a low-pressure steam output pipeline (26); the heat medium of the light component removal tower reboiler B (14) is the tower bottom material of the isobutene light component removal tower (12); and the low-pressure steam output pipeline (26) is provided with a pipeline connected with the condensate cooler (3).

4. The apparatus for producing isobutylene by cracking methyl tert-butyl ether according to claim 3, wherein The condensate cooler (3) is provided with a coolant inlet, a coolant outlet, a heat medium inlet and a heat medium outlet; the coolant of the condensate cooler (3) is steam condensate; and the heat medium is the gas generated by the cracking of the cracking reactor (2); the gas generated by the cracking of the cracking reactor (2) enters the condensate cooler (3) through the heat medium inlet, is cooled and then connected with the circulating water cooler (4) through the heat medium outlet; the coolant outlet of the condensate cooler (3) is connected with the light component removal tower reboiler A (13); and the light component removal tower reboiler A (13) is provided with a pipeline connected with the coolant inlet of the condensate cooler (3).

5. The apparatus for the production of isobutene by the cracking of methyl tert-butyl ether according to claim 4, characterized in that, The steam condensate is used as the heat medium of the light component removal tower reboiler A (13) after heat exchange in the condensate cooler (3), is circulated to the coolant inlet of the condensate cooler (3) after heat exchange in the light component removal tower reboiler A (13) and used as the coolant, and the coolant of the light component removal tower reboiler A (13) is the tower bottom material of the isobutene light component removal tower (12).

6. The apparatus for the production of isobutylene by the cracking of methyl tert-butyl ether according to claim 1, characterized in that, The upper part of the absorption cooling tower (5) is connected with the extractant pipeline (28), the bottom part of the absorption cooling tower (5) is provided with a pipeline connected with the methanol recovery tower (6), the bottom part of the methanol recovery tower (6) is provided with a pipeline returning to the upper part of the absorption cooling tower (5), and the top part of the methanol recovery tower (6) is connected with the methanol refining tower (7).

7. The apparatus for the production of isobutene by the cracking of methyl tert-butyl ether according to claim 6, characterized in that, The top part of the methanol refining tower (7) is provided with a pipeline connected with the compressor inlet buffer tank (8), and the bottom part is connected with the methanol pipeline (20).

8. The apparatus for the production of isobutylene by the cleavage of methyl tert-butyl ether according to claim 1, characterized in that, The upper part of the isobutene water washing tower (10) is connected with the desalted water pipeline (22), and the bottom part is connected with the sewage pipeline (21).

9. The apparatus for the production of isobutylene by the cracking of methyl tert-butyl ether according to claim 1, characterized in that, The bottom parts of the compressor inlet buffer tank (8) and the isobutene feed buffer tank (11) are both provided with pipelines connected with the water bag collecting tank (16), and the water bag collecting tank (16) is provided with a pipeline connected with the absorption cooling tower (5).

10. The apparatus for the production of isobutylene by the cleavage of methyl tert-butyl ether according to claim 1, characterized in that, The bottom part of the isobutene heavy carbon four pipeline (24) is connected with the heavy carbon four pipeline (24).

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