A disproportionation and transalkylation system

Abstract

The utility model discloses a disproportionation and alkyl transfer system, including partition wall tower, first heat exchanger, bleeder gas absorption tower, caly tower and through pipeline order connection's heater, disproportionation and alkyl transfer reactor, air cooler, reaction product separator, the partition wall tower includes tower body and the first vertical baffle and the second vertical baffle of being located in the tower body and being along the vertical interval distribution, to separate and form the feeding stripping zone, reflux zone, upper common area, aromatic extraction product pre -fractionation zone, toluene side area and lower common area in the tower body, and the inlet of heater communicates with the discharge port of mixed raw material feeding pipeline, the inlet of caly tower communicates with the discharge port of aromatic extraction product pipeline. The present application can recover hydrogen in bleeder gas to reduce the consumption of high-purity hydrogen, and simplify the reaction product separation process, thereby saving energy and reducing production cost.

Description

Technical Field

[0001] This utility model relates to the field of chemical equipment technology, and in particular to a disproportionation and alkyl transfer system. Background Technology

[0002] The disproportionation and alkyl transfer process using C7 or C9 / C10 aromatics as mixed feedstocks includes disproportionation and alkyl transfer reaction steps and reaction product separation steps. This process can yield high-value single products (such as ethane-rich gas, crude benzene, pure benzene, toluene, etc.).

[0003] Specifically, in the disproportionation and alkyl transfer reaction process, it is necessary to ensure that the circulating hydrogen has sufficient purity. Currently, the common method is to continuously discharge a certain amount of circulating hydrogen (purge gas) while continuously replenishing high-purity hydrogen. In the reaction product separation process, the commonly used method is to separate the reaction products into ethane-rich gas, crude benzene, pure benzene, toluene, and C8+ components by passing them through four distillation columns: a disproportionation stripping column, a benzene column, a toluene column, and a crude benzene stripping column. Utility Model Content

[0004] To enrich the product range of disproportionation and alkyl transfer systems and increase the selection space for disproportionation and alkyl transfer systems, this utility model provides a disproportionation and alkyl transfer system.

[0005] This utility model proposes a disproportionation and alkyl transfer system, comprising: To achieve the above objectives, this utility model proposes a disproportionation and alkyl transfer system, comprising: a partition wall tower, a first heat exchanger, a purge gas absorption tower, a clay tower, and a heater, a disproportionation and alkyl transfer reactor, an air cooler, and a reaction product separator connected sequentially by pipelines. The partition wall tower includes a tower body and a first vertical partition and a second vertical partition arranged vertically at intervals within the tower body. The upper end of the first vertical partition is connected to the top of the inner sidewall of the tower body, so that a feed stripping zone and a reflux zone are formed on the left and right sides of the first vertical partition in the tower body, respectively. An upper common area is formed between the first vertical partition and the second vertical partition. An aromatic extraction product pre-fractionation zone and a toluene side-collection zone are formed on the left and right sides of the second vertical partition, respectively. The lower end of the second vertical partition is spaced apart from the bottom of the inner sidewall of the tower body, and a lower common area is formed in the spaced area. The inlet of the heater is connected to the outlet of the mixed raw material feed pipeline. The gas phase outlet of the reaction product separator is connected to the mixed raw material feed pipeline through a first pipeline. The first pipeline is connected to the gas phase inlet at the bottom of the purge gas absorption tower through a first branch pipeline. The gas phase outlet at the top of the purge gas absorption tower is connected to the mixed raw material feed pipeline through a second branch pipeline. The liquid phase outlet of the reaction product separator is connected to the cold side inlet of the first heat exchanger through a second pipeline. The cold side outlet of the first heat exchanger is connected to the feed stripping zone. The lower common zone is connected to the hot side inlet of the first heat exchanger through a third pipeline. The hot side outlet of the first heat exchanger is connected to the liquid phase inlet at the top of the purge gas absorption tower. The inlet of the clay tower is connected to the outlet of the aromatic extraction product pipeline, and the outlet of the clay tower is connected to the pre-fractionation zone of the aromatic extraction product. The feed stripping zone is connected to an ethane-rich gas extraction pipeline and a crude benzene extraction pipeline, the reflux zone is connected to a pure benzene extraction pipeline, and the toluene side extraction zone is connected to a toluene extraction pipeline.

[0006] Optionally, the liquid phase outlet at the bottom of the purge gas tower is connected to the second pipeline via a third branch pipeline.

[0007] Optionally, the outlet of the toluene extraction pipeline is connected to the mixed feedstock pipeline.

[0008] Optionally, the system also includes a top condenser, wherein the top of the reflux zone is connected to the inlet of the top condenser via a distillate collection line, and the outlet of the top condenser is connected to the side of the reflux zone via a distillate reflux line.

[0009] Optionally, it also includes a bottom reboiler, the bottom of the lower common area being connected to the inlet of the bottom reboiler via a pipeline, and the outlet of the bottom reboiler being connected to the side of the toluene-side mining area via a pipeline.

[0010] Optionally, it also includes a liquid phase extraction pipeline for the interstitial tower, the inlet of which is connected to the third pipeline.

[0011] Optionally, it also includes a second heat exchanger, wherein the inlet of the mixed raw material feed line is connected to the cold side inlet of the second heat exchanger, the cold side outlet of the heat exchanger is connected to the inlet of the heater, the outlet of the disproportionation and alkyl transfer reactor is connected to the hot side inlet of the second heat exchanger, and the hot side outlet of the second heat exchanger is connected to the inlet of the air cooler.

[0012] Optionally, the first pipeline is equipped with a circulating hydrogen compressor.

[0013] Optionally, the ethane-rich gas extraction pipeline is equipped with an ethane-rich gas compressor.

[0014] Optionally, it also includes a supplementary hydrogen inlet pipeline, the outlet of which is connected to the first pipeline, and the second branch pipeline is connected between the gas phase outlet at the top of the purge gas absorption tower and the supplementary hydrogen inlet pipeline.

[0015] Optionally, the supplemental hydrogen inlet line is equipped with a supplemental hydrogen compressor.

[0016] The beneficial effects of the above-mentioned technical solutions provided by the embodiments of this utility model include at least the following: The disproportionation and alkyl transfer system provided by this invention separates the reaction products in a reaction product separator. Part of the gaseous purge gas enters the mixed feed pipeline through the first pipeline as circulating hydrogen to continue participating in the reaction, while the other part enters the purge gas absorption tower through the first branch pipeline. The C8+ component entering the purge gas absorption tower from the lower common area of ​​the partition wall tower acts as a lean absorbent to absorb non-hydrogen components in the purge gas to purify the hydrogen. The purified hydrogen is then used as supplementary hydrogen and enters the mixed feed pipeline through the second branch pipeline. This reduces the amount of high-purity hydrogen used outside the system and greatly improves the utilization efficiency of the purge gas.

[0017] The disproportionation and alkyl transfer system provided by this invention separates the reaction products in a product separator. The liquid phase products then enter a partition wall tower for further separation. Ethane-rich gas and crude benzene are extracted from the feed stripping zone via ethane-rich gas and crude benzene extraction lines, respectively. Pure benzene is extracted from the reflux zone via a pure benzene extraction line, and toluene is extracted from the toluene side extraction zone via a toluene extraction line. Thus, a single partition wall tower replaces the disproportionation stripping tower, crude benzene stripping tower, benzene tower, and toluene tower in a traditional disproportionation unit, saving equipment investment and reducing energy consumption for heat exchange. The recovered ethane-rich gas can be used as a high-quality feedstock for ethylene cracking, while other products such as benzene are also recovered. Furthermore, the C8+ component separated from the liquid phase products after the reaction can flow from the lower common area to the top of the purge gas absorber, serving as a lean absorbent for purge gas purification, greatly improving the utilization efficiency of the reaction products.

[0018] The disproportionation and alkyl transfer system provided by this invention requires the liquid phase product to be heated to a certain temperature before entering the partition wall tower to meet separation conditions, while the C8+ component entering the purge gas absorber also needs to be cooled to be used as an absorbent. By adding a first heat exchanger, the liquid phase product before entering the partition wall tower and the C8+ component before entering the purge gas absorber can exchange heat, meeting their respective temperature requirements, thereby achieving energy recovery and utilization, resulting in energy conservation and environmental protection. Attached Figure Description

[0019] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on the structures shown in these drawings without creative effort.

[0020] Figure 1 This is a schematic diagram of the structure of a disproportionation and alkyl transfer system provided by this utility model.

[0021] Explanation of icon numbers: 100-Disproportionation and alkyl transfer system; 1-Second heat exchanger; 2-Heater; 3-Disproportionation and alkyl transfer reactor; 4-Air cooler; 5-Reaction product separator; 6-Indirect wall tower; 61-Tower body; 62-First vertical baffle; 63-Second vertical baffle; 64-Feed stripping zone; 65-Reflux zone; 66-Upper common zone; 67-Aromatics extraction product pre-fractionation zone; 68-Toluene side-collection zone; 69-Lower common zone; 7-First heat exchanger; 8-Purge gas absorption tower; 9-Clay tower; 10-Top condenser; 11-Bottom reboiler; 12-Circulating hydrogen compressor; 13-Ethane-rich gas compressor; 14-Supplementary hydrogen compressor; 15-Mixed feedstock pipeline; 16-First pipeline; 17-First branch pipeline; 18-Second branch pipeline; 19-Second pipeline; 20-Third pipeline; 21-Aromatics extraction product pipeline; 22-Ethane-rich gas extraction pipeline; 23-Crude benzene extraction pipeline; 24-Pure benzene extraction pipeline; 25-Toluene extraction pipeline; 26-Third branch pipeline; 27-Distillate extraction pipeline; 28-Distillate reflux pipeline; 29-Liquid phase extraction pipeline of the indirect wall tower; 30-Supplemental hydrogen inlet pipeline.

[0022] The realization of the purpose, functional features and advantages of this utility model will be further explained in conjunction with the embodiments and with reference to the accompanying drawings. Detailed Implementation

[0023] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the protection scope of the present utility model.

[0024] It should be noted that if the embodiments of this utility model involve directional indicators (such as up, down, left, right, front, back, etc.), the directional indicators are only used to explain the relative positional relationship and movement of the components in a certain specific posture (as shown in the figure). If the specific posture changes, the directional indicators will also change accordingly.

[0025] Furthermore, if the embodiments of this utility model involve descriptions such as "first" or "second," these descriptions are for descriptive purposes only and should not be construed as indicating or implying their relative importance or implicitly specifying the number of technical features indicated. Therefore, a feature defined with "first" or "second" may explicitly or implicitly include at least one of those features. Additionally, the meaning of "and / or" throughout the text includes three parallel solutions; for example, "A and / or B" includes solution A, solution B, or a solution where both A and B are satisfied simultaneously. Furthermore, the technical solutions of the various embodiments can be combined with each other, but this must be based on the ability of those skilled in the art to implement them. When the combination of technical solutions is contradictory or impossible to implement, it should be considered that such a combination of technical solutions does not exist and is not within the scope of protection claimed by this utility model.

[0026] The inventors discovered that in the disproportionation and alkyl transfer reaction process, the emitted purge gas generally has two destinations: one is as low-value fuel gas, and the other is to recover hydrogen from it using a pressure swing adsorption (PSA) device. However, using purge gas as fuel gas represents a low-value utilization of high-value materials. While recovering hydrogen from it using a PSA device can recover high-value hydrogen to some extent, the PSA device has high energy consumption, high recovery costs, and low recovery rates. Furthermore, in the reaction product separation process, the currently common method involves separating the reaction products through four distillation columns: a disproportionation stripping column, a benzene column, a toluene column, and a crude benzene stripping column. This results in a large number of distillation columns, leading to high costs, large footprint, and complex and costly energy recovery and heat exchange processes.

[0027] To at least partially solve the aforementioned technical problems, the inventors attempted to design a disproportionation and alkyl transfer system. This system involves adding a purge gas absorption tower to purify a portion of the purge gas before using it as supplementary hydrogen in the mixed feed line. A partition wall tower replaces the traditional disproportionation stripping tower, crude benzene stripping tower, benzene tower, and toluene tower. By adding a first heat exchanger, heat exchange occurs between the liquid product entering the partition wall tower and the C8+ component entering the purge gas absorption tower, meeting their respective temperature requirements. This reduces the amount of high-purity hydrogen used outside the system, saving costs, improves the utilization efficiency of the purge gas and the overall energy recovery effect of the system, and significantly reduces production costs.

[0028] Based on this, the present invention provides a disproportionation and alkyl transfer system. Figure 1 Specific embodiments of the disproportionation and alkyl transfer system provided by this utility model.

[0029] Please see Figure 1 The present invention provides a disproportionation and alkyl transfer system 100 comprising a partition wall tower 6, a first heat exchanger 7, a purge gas absorption tower 8, a clay tower 9, and a heater 2, a disproportionation and alkyl transfer reactor 3, an air cooler 4, and a reaction product separator 5 connected sequentially by pipelines.

[0030] The partition wall tower 6 includes a tower body 61 and a first vertical partition 62 and a second vertical partition 63 arranged vertically at intervals within the tower body 61. The upper end of the first vertical partition 62 is connected to the top of the inner wall of the tower body 61, so that a feed stripping zone 64 and a reflux zone 65 are formed on the left and right sides of the first vertical partition 62 within the tower body 61, respectively. An upper common area 66 is formed between the first vertical partition 62 and the second vertical partition 63. An aromatic extraction product pre-fractionation zone 67 and a toluene side-collection zone 68 are formed on the left and right sides of the second vertical partition 63, respectively. The lower end of the second vertical partition 63 is spaced apart from the bottom of the inner wall of the tower body 61, and a lower common area 69 is formed in the spaced area.

[0031] The inlet of the heater 2 is connected to the outlet of the mixed raw material feed pipeline 15. The gas phase outlet of the reaction product separator 5 is connected to the mixed raw material feed pipeline 15 through a first pipeline 16. The first pipeline 16 is connected to the gas phase inlet at the bottom of the purge gas absorption tower 8 through a first branch pipeline 17. The gas phase outlet at the top of the purge gas absorption tower 8 is connected to the mixed raw material feed pipeline 15 through a second branch pipeline 18. The liquid phase outlet of the reaction product separator 5 is connected to the cold side inlet of the first heat exchanger 7 through a second pipeline 19. The cold side outlet of the first heat exchanger 7 is connected to the feed stripping zone 64. The lower common zone 69 is connected to the hot side inlet of the first heat exchanger 7 through a third pipeline 20. The hot side outlet of the first heat exchanger 7 is connected to the liquid phase inlet at the top of the purge gas absorption tower 8.

[0032] The inlet of the clay tower 9 is connected to the outlet of the aromatics extraction product pipeline 21, and the outlet of the clay tower 9 is connected to the aromatics extraction product pre-fractionation zone 67. The feed stripping zone 64 is connected to an ethane-rich gas extraction pipeline 22 and a crude benzene extraction pipeline 23. The reflux zone 65 is connected to a pure benzene extraction pipeline 24, and the toluene side extraction zone 68 is connected to a toluene extraction pipeline 25.

[0033] The disproportionation and alkyl transfer system 100 provided by this utility model, after the reaction products are separated by the reaction product separator 5, part of the gas phase purge gas enters the mixed raw material feed line 15 through the first pipeline 16 as circulating hydrogen to continue participating in the reaction, and the other part enters the purge gas absorption tower 8 through the first branch pipeline 17. The C8+ component entering the purge gas absorption tower 8 from the lower common area 69 of the partition wall tower 6 will act as a lean absorbent to absorb the non-hydrogen components in the purge gas to achieve hydrogen purification. The purified hydrogen is used as supplementary hydrogen and enters the mixed raw material feed line 15 through the second branch pipeline 18, which reduces the amount of high-purity hydrogen used outside the system and greatly improves the utilization efficiency of hydrogen in the purge gas.

[0034] The disproportionation and alkyl transfer system 100 provided by this utility model, after the reaction products are separated by the reaction product separator 5, the liquid phase products enter the indirect wall tower 6 for further separation. Ethane-rich gas and crude benzene in the products are extracted from the feed stripping zone 64 through ethane-rich gas extraction line 22 and crude benzene extraction line 23, respectively. Pure benzene is extracted from the reflux zone 65 through the pure benzene extraction line 24, and toluene is extracted from the toluene side extraction zone 68 through the toluene extraction line 25. Thus, by replacing the disproportionation stripping tower, crude benzene stripping tower, benzene tower, and toluene tower in a traditional disproportionation unit with a single indirect wall tower 6, equipment investment is saved, and energy consumption required for heat exchange is reduced. The recovered ethane-rich gas can be used as a high-quality feedstock for ethylene cracking, while other products such as benzene are also recovered. Furthermore, the C8+ component separated from the liquid phase products after the reaction can flow from the lower common zone 69 into the top of the purge gas absorption tower 8 as a lean absorbent for purge gas purification, greatly improving the utilization efficiency of the reaction products.

[0035] The disproportionation and alkyl transfer system 100 provided by this invention addresses the issue that the liquid phase product needs to be heated to a certain temperature before entering the partition wall tower 6 to meet separation conditions, while the C8+ component entering the purge gas absorption tower 8 also needs to be cooled to be used as an absorbent. By adding a first heat exchanger 7, heat exchange can be performed between the liquid phase product before entering the partition wall tower 6 and the C8+ component before entering the purge gas absorption tower 8, satisfying their respective temperature requirements and thus achieving energy recovery and utilization, resulting in energy conservation and environmental protection.

[0036] It should be noted that the non-hydrogen components of the purge gas are mainly C2-C5 alkanes, and contain small amounts of benzene and other components. The C2-C5 alkanes are high-quality ethylene cracking feedstocks, and benzene is a high-value chemical raw material.

[0037] See Figure 1 The process of the disproportionation and alkyl transfer system 100 provided by this utility model is as follows: A mixture of C7 or C9 / C10 aromatics is fed into heater 2 via mixed feed line 15 to reach the required reaction temperature. It then enters disproportionation and alkyl transfer reactor 3 for reaction. The reaction product is cooled by air cooler 4 and then separated into gas and liquid phases in product separator 5. Part of the purge gas is returned to mixed feed line 15 via first line 16 as circulating hydrogen for further reaction, while another part of the purge gas enters purge gas absorption tower 8 via first branch line 17. The hydrogen purified by purge gas absorption tower 8 is returned to mixed feed line 15 via second branch line 18 as supplementary hydrogen for further reaction. The liquid phase product enters the feed stripping zone 64 through the cold side of the first heat exchanger 7. The aromatic extraction products (benzene and toluene) enter the aromatic extraction product pre-fractionation zone 67 through the clay tower 9. The clay tower 9 is used to remove trace amounts of unsaturated hydrocarbons such as olefins and carbonyl groups and impurities from the aromatic extraction products, i.e., benzene and toluene, to ensure the purity and quality of the subsequent products. Benzene and toluene, as light components, will flow upward as a gas stream and counter-currently flow with the liquid phase stream entering the feed stripping zone 64 through the second pipeline 19. A portion of the benzene and toluene gas stream enters the feed stripping zone 64. Lighter ethane-rich gas is extracted from the top of the feed stripping zone 64 through the ethane-rich gas extraction pipeline 22, and crude benzene is extracted from the side of the feed stripping zone 64 through the crude benzene extraction pipeline 23 (the feed stripping zone 64 is equivalent to a separate stripping tower, with ethane-rich gas enriched at the top, benzene enriched in the middle, and toluene enriched at the bottom). Toluene and xylene from the liquid stream in feed stripping zone 64 flow downwards into aromatics extraction product pre-fractionation zone 67. The heavier xylene then enters the lower common zone 69 (aromatics extraction product pre-fractionation zone 67 is equivalent to a separate stripping tower, with toluene enriched at the top and xylene enriched at the bottom). Another portion of the benzene and toluene gas stream passes through the upper common zone 66, where it flows counter-currently with the liquid stream from reflux zone 65. Benzene, as the lighter component, enters reflux zone 65 and is extracted through the pure benzene extraction line 24 on the side of reflux zone 65 (reflux zone 65 is equivalent to a separate stripping tower, with benzene enriched at the top and toluene enriched at the bottom). Toluene flows downwards into toluene-side extraction zone 68, where it is extracted through toluene extraction line 25 (toluene-side extraction zone 68 is equivalent to a separate stripping tower, with toluene enriched at the top and xylene enriched at the bottom). The C8+ components (including xylene, etc.) in the lower public area 69 enter the top of the purge gas absorption tower 8 through the third pipeline 20 and the hot side of the first heat exchanger 7, and act as a lean absorbent to absorb the non-hydrogen components in the purge gas.

[0038] It should be noted that the aromatic extraction product is extracted by an external aromatic extraction device, which can provide the system with raw materials that can produce disproportionation and alkyl transfer reactions, and generate high-value chemical raw materials through these reactions.

[0039] The following will describe, by way of example, further specific implementations or refinements of the disproportionation and alkyl transfer system 100, in order to further improve its efficiency, reliability or for other improvements.

[0040] As previously described, the C8+ component in the lower common area 69 enters the top of the purge gas absorption tower 8 via the third pipeline 20 and the hot side of the first heat exchanger 7, serving as a lean absorbent. After absorbing the non-hydrogen components in the purge gas, this lean absorbent flows to the bottom of the purge gas absorption tower 8, becoming a rich absorbent. To improve the utilization rate of this rich absorbent, in some embodiments, the liquid phase outlet at the bottom of the purge gas absorption tower 8 is connected to the second pipeline 19 via a third branch pipeline 26. Thus, the liquid C8+ component at the bottom of the purge gas absorption tower 8 re-enters the partition tower 6 for separation via the third branch pipeline 26 and the second pipeline 19.

[0041] It is understood that toluene is an important raw material for disproportionation and alkyl transfer reactions. To reduce the consumption of fresh raw materials, in some embodiments, the outlet of the toluene outflow line 25 is connected to the mixed feedstock line 15. In this way, the toluene outflow line 25 from the partition wall tower 6 is fed into the mixed feedstock line 15 through the toluene outflow line 25 as a raw material for the reaction, thereby improving the utilization rate of the product.

[0042] Considering that the distillation separation within the partition wall column 6 is primarily achieved through countercurrent mass transfer of the gas and liquid phases, some embodiments further include a top condenser 10. The top of the reflux zone 65 is connected to the inlet of the top condenser 10 via a distillate collection line 27, and the outlet of the top condenser 10 is connected to the side of the reflux zone 65 via a distillate reflux line 28. Thus, the top condenser 10 can condense the gas concentrated at the top of the reflux zone 65 to provide a sufficient downward liquid stream. In some embodiments, a bottom reboiler 11 is also included. The bottom of the lower common zone 69 is connected to the inlet of the bottom reboiler 11 via a pipeline, and the outlet of the bottom reboiler 11 is connected to the side of the toluene side collection zone 68 via a pipeline. Thus, the bottom reboiler 11 can heat and evaporate the liquid concentrated in the lower common zone 69 to provide a sufficient upward gas stream.

[0043] In some embodiments, a partition wall tower liquid phase extraction line 29 is also included, the inlet of which is connected to the third line 20. Thus, if necessary, a portion of the C8+ component within the lower common area 69 can be extracted through the partition wall tower liquid phase extraction line 29.

[0044] To improve the energy recovery efficiency of the entire system, some embodiments further include a second heat exchanger 1. The inlet of the mixed raw material feed line 15 is connected to the cold-side inlet of the second heat exchanger 1, the cold-side outlet of the heat exchanger is connected to the inlet of the heater 2, the outlet of the disproportionation and alkyl transfer reactor 3 is connected to the hot-side inlet of the second heat exchanger 1, and the hot-side outlet of the second heat exchanger 1 is connected to the inlet of the air cooler 4. Thus, through the second heat exchanger 1, the mixed raw material entering the cold side of the second heat exchanger 1 and the reaction products entering the hot side of the second heat exchanger 1 can exchange heat, thereby reducing the energy consumption of the heater 2 and the air cooler 4 and lowering production costs.

[0045] In some embodiments, to continuously supply sufficient hydrogen to the disproportionation and alkyl transfer reactor 3, the first pipeline 16 is equipped with a circulating hydrogen compressor 12. Specifically, the outlet of the circulating hydrogen compressor 12 is located near the mixed feedstock pipeline 15. Similarly, to continuously extract ethane-rich gas from the system, the ethane-rich gas extraction pipeline 22 is equipped with an ethane-rich gas compressor 13. Specifically, the inlet of the ethane-rich gas compressor 13 is located near the partition tower 6.

[0046] Considering that the amount of hydrogen purified by the purge gas absorption tower 8 gradually decreases with increasing reaction time, in order to ensure the stable operation of the entire system for a long period of time, some embodiments also include a supplementary hydrogen inlet line 30. The outlet of the supplementary hydrogen inlet line 30 is connected to the first line 16, and the second branch line 18 is connected between the gas phase outlet at the top of the purge gas absorption tower 8 and the supplementary hydrogen inlet line 30. In this way, hydrogen can be supplied to the system from the outside through the supplementary hydrogen inlet line 30 to continuously complete the efficient and stable reaction. In order to continuously provide supplementary hydrogen to the system, in some embodiments, the supplementary hydrogen inlet line 30 is equipped with a supplementary hydrogen compressor 14. Specifically, the outlet of the supplementary hydrogen compressor 14 is located close to the mixed raw material feed line 15.

[0047] The above description is only a preferred embodiment of the present utility model and does not limit the patent scope of the present utility model. All equivalent structural transformations made under the concept of the present utility model and using the contents of the present utility model specification and drawings, or direct / indirect applications in other related technical fields, are included in the patent protection scope of the present utility model.

Claims

1. A disproportionation and transalkylation system characterized by, include: The components include a partition wall tower, a first heat exchanger, a purge gas absorption tower, a clay tower, and a heater, a disproportionation and alkyl transfer reactor, an air cooler, and a reaction product separator connected sequentially by pipelines. The partition wall tower includes a tower body and a first vertical partition and a second vertical partition arranged vertically at intervals within the tower body. The upper end of the first vertical partition is connected to the top of the inner sidewall of the tower body, so that a feed stripping zone and a reflux zone are formed on the left and right sides of the first vertical partition in the tower body, respectively. An upper common area is formed between the first vertical partition and the second vertical partition. An aromatic extraction product pre-fractionation zone and a toluene side-collection zone are formed on the left and right sides of the second vertical partition, respectively. The lower end of the second vertical partition is spaced apart from the bottom of the inner sidewall of the tower body, and a lower common area is formed in the spaced area. The inlet of the heater is connected to the outlet of the mixed raw material feed pipeline. The gas phase outlet of the reaction product separator is connected to the mixed raw material feed pipeline through a first pipeline. The first pipeline is connected to the gas phase inlet at the bottom of the purge gas absorption tower through a first branch pipeline. The gas phase outlet at the top of the purge gas absorption tower is connected to the mixed raw material feed pipeline through a second branch pipeline. The liquid phase outlet of the reaction product separator is connected to the cold side inlet of the first heat exchanger through a second pipeline. The cold side outlet of the first heat exchanger is connected to the feed stripping zone. The lower common zone is connected to the hot side inlet of the first heat exchanger through a third pipeline. The hot side outlet of the first heat exchanger is connected to the liquid phase inlet at the top of the purge gas absorption tower. The inlet of the clay tower is connected to the outlet of the aromatic extraction product pipeline, and the outlet of the clay tower is connected to the pre-fractionation zone of the aromatic extraction product. The feed stripping zone is connected to an ethane-rich gas extraction pipeline and a crude benzene extraction pipeline, the reflux zone is connected to a pure benzene extraction pipeline, and the toluene side extraction zone is connected to a toluene extraction pipeline.

2. The disproportionation and transalkylation system of claim 1, wherein, The liquid phase outlet at the bottom of the purge gas absorption tower is connected to the second pipeline via a third branch pipeline.

3. The disproportionation and transalkylation system of claim 1, wherein, The outlet of the toluene extraction pipeline is connected to the mixed raw material feed pipeline.

4. The disproportionation and alkyl transfer system as described in claim 1, characterized in that, It also includes a top condenser, the top of the reflux zone is connected to the inlet of the top condenser via a distillate collection line, and the outlet of the top condenser is connected to the side of the reflux zone via a distillate reflux line.

5. The disproportionation and transalkylation system of claim 1 or 4, wherein It also includes a bottom reboiler, the bottom of the lower common area is connected to the inlet of the bottom reboiler via a pipeline, and the outlet of the bottom reboiler is connected to the side of the toluene side mining area via a pipeline.

6. The disproportionation and alkyl transfer system as described in claim 1, characterized in that, It also includes a liquid phase extraction pipeline for the inter-wall tower, the inlet of which is connected to the third pipeline.

7. The disproportionation and alkyl transfer system as described in claim 1, characterized in that, It also includes a second heat exchanger, wherein the inlet of the mixed raw material feed pipeline is connected to the cold side inlet of the second heat exchanger, the cold side outlet of the heat exchanger is connected to the inlet of the heater, the outlet of the disproportionation and alkyl transfer reactor is connected to the hot side inlet of the second heat exchanger, and the hot side outlet of the second heat exchanger is connected to the inlet of the air cooler.

8. The disproportionation and transalkylation system of claim 1, wherein, The first pipeline is equipped with a circulating hydrogen compressor.

9. The disproportionation and transalkylation system of claim 1, wherein, The ethane gas extraction pipeline is equipped with an ethane gas compressor.

10. The disproportionation and transalkylation system of claim 1, wherein, It also includes a supplementary hydrogen inlet pipeline, the outlet of which is connected to the first pipeline, and the second branch pipeline is connected between the gas phase outlet at the top of the purge gas absorption tower and the supplementary hydrogen inlet pipeline.

11. The disproportionation and transalkylation system of claim 10, wherein, The supplemental hydrogen inlet line is equipped with a supplemental hydrogen compressor.

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