A divided oil rich debenzolizing column

Abstract

This invention relates to a rich-oil benzene removal tower for fractional distillation, specifically in the field of benzene removal tower technology. It includes a reboiler, a tower body, and a tower top. One side of the tower body is connected to a rich-oil pipeline and a steam pipeline, while the other side is connected to a naphthalene oil collection tank. A partition plate for separation is installed inside the tower body, with a receiving tray and downcomer on both sides of the partition plate to guide the liquid flow. The reboiler is connected to the tower body and is connected to a lean-oil pipeline. The tower top is connected to a crude benzene pipeline, which in turn connects to a reflux tank. The reflux tank is connected to the crude benzene storage tank and the inner cavity of the tower top. The crude benzene storage tank is connected to the tower body via a liquid phase distribution pump. In this invention, the partition plate within the tower body allows rich-oil to be fed from one side of the partition plate, while high-concentration naphthalene oil is collected from the other side. The benzene removal tower does not need to operate in conjunction with a naphthalene removal tower; the tower body can simultaneously remove high-concentration naphthalene oil (greater than 50%) while removing benzene, thereby reducing the naphthalene content in the lean oil and improving the naphthalene washing effect.

Description

Technical Field

[0001] This invention relates to the field of benzene removal tower technology, and specifically discloses a rich oil benzene removal tower for separate distillation. Background Technology

[0002] A benzene removal tower is a distillation device used in the wash oil absorption of crude benzene process. Benzene removal towers belong to the desorption tower category and are operational devices that allow benzene hydrocarbons dissolved in the wash oil solvent to evaporate and be released through direct contact heat transfer via a heat carrier. The naphthalene content in the wash oil has a significant impact on the removal of naphthalene from coke oven gas. High naphthalene content in the wash oil will lead to high naphthalene content in the coke oven gas, severely interfering with downstream processing and utilization of the coke oven gas.

[0003] The utility model patent with authorization announcement number CN208980676U discloses a coke oven gas treatment system, including a gas-water separation unit, a coke oven gas purification unit, a coke oven gas compression unit, a coke oven gas filtration unit, and a coke oven gas heating unit connected in sequence through a gas pipeline. The coke oven gas purification unit includes a desulfurization tower, a naphthalene removal tower, and a benzene removal tower connected in sequence along the gas flow direction. The gas inlet of the desulfurization tower is connected to the gas outlet of the gas-water separation unit, and the gas outlet of the benzene removal tower is connected to the gas inlet of the coke oven gas compression unit.

[0004] Currently, some production enterprises have naphthalene oil side streams in their rich oil benzene removal towers, which can control the naphthalene content in lean oil to some extent. However, due to the unclear fractionation of various fractions in conventional side stream distillation towers, the naphthalene content in the naphthalene oil side stream is low (usually below 30%), resulting in a significant loss of methylnaphthalene and severely affecting the benzene washing effect of the circulating lean oil. In publicly available patented technologies, connecting a naphthalene removal tower to the benzene removal tower can guarantee the naphthalene content ratio in the naphthalene oil side stream. However, constructing a naphthalene removal tower (naphthalene washing tower) greatly increases the enterprise's construction costs, leading to higher overall investment costs for production equipment and increased energy consumption, which is detrimental to the long-term development of the enterprise. Summary of the Invention

[0005] In view of the problem that the current benzene removal tower production line has high equipment investment and production energy consumption due to the additional construction of the naphthalene removal tower, the present invention provides a rich oil benzene removal tower for separate distillation.

[0006] To address the above problems, the present invention provides the following technical solution:

[0007] A rich-oil benzene removal column for fractional distillation includes a reboiler, a column body, and a column top. One side of the column body is connected to a rich-oil pipeline and a vapor pipeline, and the other side of the column body is connected to a naphthalene oil collection tank. A partition plate for separation is installed inside the column body, and a receiving tray and a downcomer for guiding the liquid flow are provided on both sides of the partition plate. The reboiler is connected to the column body and is connected to a lean-oil pipeline. The column top is connected to a crude benzene pipeline, which is connected to a reflux tank. The reflux tank is connected to a reflux pipeline, which is connected to a crude benzene storage tank and the inner cavity of the column top. The inner cavity of the column top is connected to the column body through a liquid phase distribution pump.

[0008] Preferably, the tower body includes a first tower body, a second tower body, and a third tower body connected in sequence; the first tower body is connected to the tower top, the third tower body is connected to the tower bottom, and the partition plate passes through the first tower body and the second tower body from top to bottom. The projection of the partition plate can be one or a combination of straight line, broken line, and arc shape; multiple layers of tower plates are uniformly installed inside the first tower body, the second tower body, the third tower body, and the tower top from top to bottom.

[0009] Preferably, the first tower body is connected to multiple naphthalene oil pipelines connected to a naphthalene oil collection tank, and a naphthalene oil extraction pump is installed on the oil outlet pipeline of the naphthalene oil collection tank.

[0010] Preferably, the upper part of the first tower body has at least two liquid inlets, each of which is connected to the liquid outlet pipe of the liquid phase distribution pump, and the liquid inlets are evenly distributed on the left and right sides of the partition plate.

[0011] Preferably, the top of the tower is provided with a gas outlet connected to a crude benzene pipeline, a condenser connected to a reflux tank is installed on the crude benzene pipeline, a reflux inlet connected to a reflux pipeline is provided on the outer wall of the tower top, and a level gauge connection port and a liquid outlet are also provided on the outer wall of the tower top, with the liquid outlet connected to the liquid inlet pipeline of the liquid phase distribution pump.

[0012] Preferably, the top of the tower is provided with a first tray and a second tray, both of which are provided with multiple layers and are arranged in a staggered manner. A first receiving tray is provided on the left side of the first tray and a first downcomer is provided on the right side of the first tray. A second downcomer is provided on the left side of the second tray and a second receiving tray is provided on the right side of the second tray.

[0013] Preferably, the interior of the first tower body is provided with a third tower plate and a fourth tower plate that are symmetrically separated by a partition plate. The third tower plate and the fourth tower plate are each provided with multiple layers that are evenly staggered vertically. The front end of the third tower plate is provided with a third downcomer and the rear end of the third tower plate is provided with a third liquid receiving tray. The front end of the fourth tower plate is provided with a fourth liquid receiving tray and the rear end of the fourth tower plate is provided with a fourth downcomer.

[0014] Preferably, the interior of the second tower body is provided with a fifth tower plate and a sixth tower plate symmetrically separated by a partition plate. The fifth tower plate and the sixth tower plate are each provided with multiple layers and are evenly staggered vertically. A fifth downcomer is provided on the fifth tower plate and the fifth downcomer is arranged on the left side of the partition plate. A rich oil inlet connected to a rich oil pipeline is opened at the upper part of the second tower body. The rich oil inlet is located above the uppermost fifth downcomer. A fifth receiving tray is provided at the front left side of the fifth tower plate, a sixth downcomer is provided at the front right side of the fifth tower plate, and a sixth receiving tray is provided at the rear end of the fifth tower plate. A seventh downcomer is provided at the front left side of the sixth tower plate, a seventh receiving tray is provided at the front right side of the sixth tower plate, and an eighth downcomer is provided at the rear end of the sixth tower plate.

[0015] Preferably, the interior of the third tower body is provided with a seventh tower plate, the seventh tower plate is provided with multiple layers, the seventh tower plates are arranged vertically and alternately from top to bottom, and a ninth downcomer is provided on each of the seventh tower plates.

[0016] Preferably, a reboiler is provided on one side of the column bottom, the top port of the reboiler is connected to the third column body, and the bottom port of the reboiler is connected to the column bottom.

[0017] Compared with the prior art, the present invention has the following beneficial effects:

[0018] 1. The partition plate inside the tower body in this invention allows rich oil to be fed from one side of the partition plate, while high-concentration naphthalene oil is collected from the other side of the partition plate. Crude benzene can be produced at the top of the tower, and lean oil can be obtained at the bottom of the tower. The benzene removal tower does not need to be operated in conjunction with the naphthalene removal tower. The tower body can collect high-concentration naphthalene oil with a concentration greater than 50% at the same time as benzene removal, thereby reducing the naphthalene content in the lean oil, thus improving the naphthalene washing effect and solving the problems of high equipment investment and high production energy consumption.

[0019] 2. In this invention, the partitions are set in various shapes, which allows enterprises to provide a variety of solutions based on their actual situation. If cost saving and practicality are the main priorities, straight partitions can be used. If it is necessary to increase production speed, broken line or arc type partitions can be used. They can also be used in combination to adapt to the various production needs of enterprises, thereby further improving the practicality and popularity of this invention.

[0020] 3. The tower body of the present invention is provided with multiple layers of tower plates, and each layer of tower plate is provided with a liquid receiving tray and a downcomer. The liquid receiving tray and downcomer can guide the reactants in the tower body in one direction, thereby ensuring the smoothness of the benzene removal tower reaction. Compared with the benzene removal tower in the prior art, the benzene removal tower of the present invention has a smoother reaction rate, thereby making the output efficiency of the benzene removal tower higher and improving the production efficiency of enterprises.

[0021] 4. The present invention has a liquid phase distribution pump installed between the top of the tower and the tower body, which can evenly transport crude benzene to both sides of the partition plate, avoid the loss of methyl naphthalene, ensure that the naphthalene content in the naphthalene oil meets the production standard, and at the same time further reduce the naphthalene content of the lean oil, ensuring that the lean oil output from the benzene removal tower can be used in the production process of other equipment. Therefore, it has a very wide range of application prospects. Attached Figure Description

[0022] To more clearly illustrate the technical solution of the present invention, the drawings used in the description will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0023] Figure 1 This is a schematic diagram of the overall structure of the benzene removal tower of the present invention;

[0024] Figure 2 This is a schematic diagram of the internal structure of the tower top of the present invention;

[0025] Figure 3 This is a schematic diagram of the first tower structure of the present invention;

[0026] Figure 4 This is a schematic diagram of the second tower structure of the present invention;

[0027] Figure 5 This is a schematic diagram of the third tower structure of the present invention;

[0028] Figure 6 This is a schematic diagram of the arrangement structure of the first liquid receiving plate and the first downcomer of the present invention;

[0029] Figure 7 This is a schematic diagram of the arrangement structure of the second downcomer and the second receiving plate of the present invention;

[0030] Figure 8 This is a schematic diagram of the arrangement structure of the third downcomer and the third receiving plate of the present invention;

[0031] Figure 9 This is a schematic diagram of the arrangement structure of the fourth liquid receiving plate and the fourth downcomer of the present invention;

[0032] Figure 10 This is a schematic diagram of the arrangement structure of the fifth downcomer, the fifth receiving plate, the sixth downcomer, and the sixth receiving plate of the present invention.

[0033] Figure 11 This is a schematic diagram of the arrangement structure of the seventh downcomer, the seventh receiving plate, and the eighth downcomer of the present invention.

[0034] Figure 12This is a schematic diagram of the ninth downcomer arrangement structure of the present invention. Figure 1 ;

[0035] Figure 13 This is a schematic diagram of the ninth downcomer arrangement structure of the present invention. Figure 2 ;

[0036] Figure 14 This is a schematic diagram of the linear partition plate structure of the present invention;

[0037] Figure 15 This is a schematic diagram of the broken-line type partition plate structure of the present invention;

[0038] Figure 16 This is a schematic diagram of the arc-shaped partition plate structure of the present invention;

[0039] In the diagram: 1. Reboiler, 2. Tower body, 201. First tower body, 202. Second tower body, 203. Third tower body, 204. Liquid inlet, 205. Rich oil feed inlet, 3. Tower top, 301. Gas outlet, 302. Reflux inlet, 303. Level gauge connection port, 304. Liquid outlet, 4. Rich oil pipeline, 5. Steam pipeline, 6. Naphthalene oil collection tank, 7. Divider plate, 8. Lean oil pipeline, 9. Crude benzene pipeline, 10. Reflux tank, 11. Reflux pipeline, 12. Crude benzene storage tank, 13. Liquid phase distribution pump, 14. Naphthalene oil pipeline, 15. Naphthalene oil production pump, 16. First tower plate, 17. Second tray, 18. First receiving tray, 19. First downcomer, 20. Second downcomer, 21. Second receiving tray, 22. Third tray, 23. Fourth tray, 24. Third downcomer, 25. Third receiving tray, 26. Fourth receiving tray, 27. Fourth downcomer, 28. Fifth tray, 29. Sixth tray, 30. Fifth downcomer, 31. Fifth receiving tray, 32. Sixth downcomer, 33. Sixth receiving tray, 34. Seventh downcomer, 35. Seventh receiving tray, 36. Eighth downcomer, 37. Seventh tray, 38. Ninth downcomer, 39. Reboiler, 40. Condenser. Detailed Implementation

[0040] To make the objectives, features, and advantages of this invention more apparent and understandable, the technical solutions of this invention will be clearly and completely described below with reference to the accompanying drawings of the specific embodiments. Obviously, the embodiments described below are only some embodiments of this invention, and not all embodiments. Based on the embodiments of this patent, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this patent.

[0041] This specific embodiment provides a rich-oil benzene removal tower for separated distillation, such as... Figures 1-16As shown, the structure includes a bottom column 1, a column body 2, and a top column 3. The bottom column 1 is located at the bottom of the benzene removal column and serves as its base. The column body 2 and the top column 3 are installed on the bottom column 1 from bottom to top. The column body 2 includes a first column body 201, a second column body 202, and a third column body 203 connected in sequence from top to bottom. The first column body 201 is connected to the top column 3, and the third column body 203 is connected to the bottom column 1. A rich oil pipe 4 is connected to the bottom of one side of the first column body 201, which allows rich oil to be introduced into the first column body 201. Inside the tower body 201, on the other side of the first tower body 201, there are multiple naphthalene oil pipes 14 connected to the naphthalene oil collection tank 6. After the rich oil is distilled, the resulting naphthalene oil can flow from the other side of the first tower body 201 into the naphthalene oil pipes 14, and then enter the naphthalene oil collection tank 6 for storage. By setting multiple naphthalene oil pipes 14, the extraction efficiency of naphthalene oil can be improved, and the residence time of naphthalene oil in the benzene removal tower can be effectively reduced. A naphthalene oil extraction pump 15 is installed on the oil outlet pipe of the naphthalene oil collection tank 6. The naphthalene oil extraction pump 15 can extract the naphthalene oil from the naphthalene oil collection tank 6, and then supply the naphthalene oil to the naphthalene oil processing equipment.

[0042] The top of the second tower body 202 is fixedly connected to the bottom of the first tower body 201, and the inner cavity of the second tower body 202 is connected to the inner cavity of the first tower body 201. A steam pipe 5 is connected to the side wall of the second tower body 202. The steam pipe 5 can provide high-temperature steam to the inner cavity of the second tower body 202. The high-temperature steam can enter the inner cavity of the first tower body 201 to distill the rich oil and produce naphthalene oil. By arranging the steam pipe 5 below the rich oil pipe 4, the distillation effect of the high-temperature steam can be fully utilized, allowing the rich oil in the inner cavity of the first tower body 201 to react fully. Furthermore, since the produced naphthalene oil is in a vaporized state, the high-temperature steam can lift the produced naphthalene oil, ensuring that all the naphthalene oil can enter the naphthalene oil pipe 14 and preventing the naphthalene oil from entering the second tower body 202, thus ensuring the stability of the benzene removal tower operation.

[0043] The top of the third tower body 203 is fixedly connected to the bottom of the second tower body 202. The inner cavity of the second tower body 202 is connected to the inner cavity of the third tower body 203. The inner cavity of the third tower body 203 is connected to the inner cavity of the reboiler 1. After the rich oil in the first tower body 201 undergoes distillation, lean oil is produced simultaneously. The lean oil can enter the inner cavity of the reboiler 1 through the inner cavities of the second tower body 202 and the third tower body 203. The bottom of the reboiler 1 is connected to a lean oil pipe 8, which can send the lean oil out of the benzene removal tower, thereby ensuring that the benzene removal tower can operate normally for a long time.

[0044] A reboiler 39 is provided on one side of the reboiler 1. The reboiler 39 is a vaporization device. A pipe is connected to the top and bottom of the reboiler 39. The pipe at the top of the reboiler 39 is connected to the inner cavity of the third column body 203, and the pipe at the bottom of the reboiler 39 is connected to the bottom of the reboiler 1. Part of the lean oil in the reboiler 1 enters the lean oil pipe 8, and another part of the lean oil can enter the reboiler 39. The reboiler 39 vaporizes this part of the lean oil and then passes it back into the inner cavity of the third column body 203 to further participate in the distillation of the rich oil.

[0045] A fixing plate is provided at the top of the first tower body 201. The top surface of the fixing plate is fixedly connected to the bottom of the tower top 3. The fixing plate can separate the first tower body 201 from the tower top 3. The fixing plate has a through hole, which allows the crude benzene to pass through as gaseous crude benzene is generated during the distillation process. A gas outlet 301 is provided at the top of the tower top 3. The gas outlet 301 is connected to a crude benzene pipe 9. Crude benzene can enter the crude benzene pipe 9 through the gas outlet 301. A condenser 40 is installed on the crude benzene pipe 9. The condenser 40 can liquefy the crude benzene into liquid. The crude benzene pipe 9 is connected to a reflux tank 10, where the crude benzene liquid can be stored. The reflux tank 10 is connected to a reflux pipe 11. The reflux pipe 11 has two branches. One branch is connected to a crude benzene storage tank 12, and the other branch is connected to the inner cavity of the tower top 3. The outer wall of column 3 is provided with a reflux inlet 302 connected to the reflux pipe 11. Crude benzene in the crude benzene storage tank 12 can re-enter the inner cavity of column top 3 through the reflux inlet 302. The inner cavity of column top 3 is connected to a liquid phase distribution pump 13 through a pipe. The liquid phase distribution pump 13 is connected to two liquid inlet pipes, one of which is connected to the crude benzene storage tank 12 and the other is connected to the inner cavity of column top 3. The outer wall of column top 3 is provided with a liquid outlet 304, which is fixedly connected to the liquid inlet pipe. Crude benzene in the inner cavity of column top 3 can enter the liquid phase distribution pump 13 through the liquid outlet 304. The upper part of the first column body 201 is provided with at least two liquid inlets 204, each of which is connected to the liquid outlet pipe of the liquid phase distribution pump 13. Crude benzene entering the liquid phase distribution pump 13 can enter the inner cavity of the first column body 201 through the liquid inlet 204.

[0046] The liquid outlet 304 is provided with a liquid level gauge connection port 303 on its side. The liquid level gauge connection port 303 can be connected to a liquid level gauge, which can monitor the crude benzene liquid level in the inner cavity of the top 3 of the tower in real time. If the crude benzene liquid level is too high, the crude benzene can be transported to the inner cavity of the first tower body 201 by the liquid phase distribution pump 13, thereby ensuring the normal operation of the benzene removal tower.

[0047] The top 3 of the tower is internally equipped with a first tray 16 and a second tray 17. The first tray 16 has five layers, namely 1#, 3#, 5#, 7#, and 9# in the figure. The second tray 17 also has five layers, namely 2#, 4#, 6#, 8#, and 10# in the figure. Thus, the first tray 16 and the second tray 17 are evenly staggered vertically. Each first tray 16 has a first receiving tray 18 on its left side and a first downcomer 19 on its right side. The first receiving tray 18 and the first downcomer 19 are single-flow. The structure allows the crude benzene liquid entering the inner cavity of the top 3 of the tower via the reflux pipe 11 to flow from the first receiving tray 18 to the first downcomer 19. A second downcomer 20 is provided on the left side of each second tray 17, and a second receiving tray 21 is provided on the right side of each second tray 17. The crude benzene liquid flowing through the upper first tray 16 can flow from the second receiving tray 21 to the second downcomer 20, thus forming a complete and continuous loop flow path. Finally, the crude benzene liquid can remain below the 10# second tray 17, thus facilitating the crude benzene liquid to flow out of the inner cavity of the top 3 of the tower from the outlet 304.

[0048] A partition plate 7 is provided inside the first tower body 201 and the second tower body 202. The partition plate 7 passes through the first tower body 201 and the second tower body 202 from top to bottom. The partition plate 7 can divide the inner cavity of the first tower body 201 and the second tower body 202 into two parts. The liquid inlet 204 is evenly distributed on the left and right sides of the partition plate 7. The crude benzene can be transported to the left and right sides of the partition plate 7 by the liquid phase distribution pump 13.

[0049] The first tower body 201 has a third tower plate 22 and a fourth tower plate 23 symmetrically separated by a partition plate 7. The third tower plate 22 has five layers, designated as 11#, 13#, 15#, 17#, and 19# in the figure. The fourth tower plate 23 has five layers, designated as 12#, 14#, 16#, 18#, and 20#. Thus, each layer of the third tower plate 22 and fourth tower plate 23 is evenly staggered vertically. The front end of each layer of the third tower plate 22... Each third tray 22 is equipped with a third downcomer 24. Two third downcomers 24 are arranged on each third tray 22, symmetrically distributed on the left and right sides of the partition plate 7. Each third tray 22 also has a third receiving tray 25 at its rear end. Two third receiving trays 25 are arranged on each third tray 22, symmetrically distributed on the left and right sides of the partition plate 7. The rich and lean oil entering the inner cavity of the first tower body 201 are... Oil flows from the third receiving pan 25 to the third downcomer 24 on the third tray 22, forming a unidirectional flow path. Each fourth tray 23 has a fourth receiving pan 26 at its front end, with two pans 26 arranged symmetrically on the left and right sides of the partition plate 7. Each fourth tray 23 has a fourth downcomer 27 at its rear end, with two downcomers 27 arranged symmetrically on the left and right sides of the partition plate 7. As described above, the inner cavity of the first tower body 201 is divided into two equal-volume cavities by the partition plate 7, and the flow direction of rich and lean oil in each cavity is a continuous annular flow. The presence of the third downcomer 24 and the fourth downcomer 27 connects each third tray 22 and fourth tray 23, thus forming a complete unidirectional flow path.

[0050] Since the two liquid inlets 204 are symmetrically distributed on both sides of the partition plate 7, the lean oil flow rate on both sides of the partition plate 7 can be ensured to be the same, thus ensuring the internal reaction balance of the benzene removal tower.

[0051] The interior of the second tower body 202 is provided with a fifth tower plate 28 and a sixth tower plate 29 symmetrically separated by a partition plate 7. The fifth tower plate 28 has six layers, namely 21#, 23#, 25#, 27#, 29#, and 31# in the figure. The sixth tower plate 29 has six layers, namely 22#, 24#, 26#, 28#, 30#, and 32# in the figure. It can be seen that the fifth tower plate 28 and the sixth tower plate 29 are evenly staggered vertically. A fifth downcomer is provided on both the fifth tower plate 28 and the sixth tower plate 29. 30. The fifth downcomer 30 is arranged on the left side of the partition plate 7. The upper part of the second tower body 202 is provided with a rich oil inlet 205 connected to the rich oil pipeline 4. The rich oil inlet 205 is located above the uppermost fifth downcomer 30. A fifth receiving tray 31 is provided at the left front end of each fifth tower plate 28. A sixth downcomer 32 is provided at the right front end of each fifth tower plate 28. A sixth receiving tray 33 is provided at the rear end of each fifth tower plate 28. The sixth receiving trays 31 arranged on each fifth tower plate 28 are... There are two sixth receiving trays 33, distributed on both sides of the partition plate 7. Therefore, on the left side of the partition plate 7, after the rich oil enters the inner cavity of the second tower body 202 through the rich oil inlet 205, it is affected by the fifth downcomer 30, the fifth receiving tray 31, the sixth downcomer 32, and the sixth receiving tray 33, forming multiple unidirectional flow paths: the fifth receiving tray 31 and the sixth receiving tray 33 flow to the fifth downcomer 30, and the sixth receiving tray 33 flows to the sixth downcomer 32; the left front of each sixth tower plate 29... Each of the six trays 29 has a seventh downcomer 34 at one end, a seventh receiving tray 35 at the front right side of each sixth tray 29, and an eighth downcomer 36 at the rear end of each sixth tray 29. There are two eighth downcomers 36 arranged on each sixth tray 29, and the two eighth downcomers 36 are symmetrically distributed on the left and right sides of the partition plate 7. It can be seen that the flow path on each sixth tray 29 is as follows: the fifth downcomer 30 flows to the seventh downcomer 34 and the eighth downcomer 36, and the seventh receiving tray 35 flows to the eighth downcomer 36.

[0052] The third tower body 203 has a seventh tower plate 37 inside, which has ten layers, namely 33#, 34#, 35#, 36#, 37#, 38#, 39#, 40#, 41#, and 42# in the figure. Each layer of the seventh tower plate 37 is arranged vertically and alternately from top to bottom, specifically: 33#, 35#, 37#, 39#, and 41# are arranged horizontally, and 34#, 36#, 38#, 40#, and 42# are arranged vertically. Each layer of the seventh tower plate 37 is provided with a ninth downcomer 38. By arranging the ninth downcomer 38 on the seventh tower plate 37, the lean oil flowing through each layer of the seventh tower plate 37 can be dispersed to both sides, thereby accelerating the flow rate of lean oil and improving the overall operating efficiency of the benzene removal tower.

[0053] The first tray 16, the second tray 17, the third tray 22, the fourth tray 23, the fifth tray 28, the sixth tray 29, and the seventh tray 37 are all provided with openings, which facilitate the passage of gas and liquid, thereby forming a channel that runs from top to bottom.

[0054] In addition, the projection of the partition plate 7 can be one or a combination of straight line, broken line, and arc.

[0055] Example 1

[0056] The projection of partition 7 is a straight line, such as... Figure 14 As shown, the straight-line partition plate 7 can divide its inner cavity equally, thereby ensuring that the working efficiency on both sides of the partition plate 7 is the same and ensuring the stability of the benzene removal tower; moreover, the straight-line partition plate 7 is a conventional design, the structure is relatively universal, the manufacturing process is simple, and it can save production costs.

[0057] Example 2

[0058] The projection of partition 7 is a polygonal line or an arc, such as... Figures 15-16 As shown, the bent and arc-shaped partition plates 7 are located at the center of the inner cavity, which can change the flow direction of the material above the tray, increase the flow rate, increase the gas-liquid contact area on the tray surface, and increase the distillation rate of rich oil in the benzene removal tower, thus significantly improving the production rate of the benzene removal tower.

[0059] Compared with existing technologies, this invention utilizes a partition plate within the tower body. This allows rich oil to be fed from one side of the partition plate, while high-concentration naphthalene oil is extracted from the other side. Crude benzene can be produced at the top of the tower, and lean oil can be obtained from the bottom. The benzene removal tower does not need to operate in conjunction with the naphthalene removal tower. The tower body can simultaneously extract high-concentration naphthalene oil (greater than 50%) while removing benzene, thereby reducing the naphthalene content in the lean oil and improving the naphthalene washing effect. This solves the problems of high equipment investment and high production energy consumption. Furthermore, the partition plate can be configured in various shapes, providing multiple solutions based on the company's specific needs. For cost savings and practicality, a straight partition plate can be used; for increased production speed, a zigzag or arc-shaped partition plate can be used. These can also be mixed and matched to adapt to various production requirements, further enhancing the efficiency of this invention. The invention demonstrates practicality and widespread applicability. Furthermore, the tower body is equipped with multiple layers of trays, each with a receiving pan and downcomer. These trays and downcomers provide unidirectional guidance of the reactants within the tower, ensuring a smooth reaction flow. Compared to existing benzene removal towers, the benzene removal tower of this invention exhibits a smoother reaction rate, resulting in higher output efficiency and improved production efficiency for enterprises. Finally, a liquid phase distribution pump is installed between the tower top and the tower body, allowing the crude benzene to be evenly distributed to both sides of the partition plate. This prevents the loss of methylnaphthalene, ensuring that the naphthalene content in the naphthalene oil meets production standards and further reducing the naphthalene content in lean oil, ensuring that the lean oil output from the benzene removal tower can be used in the production processes of other equipment. In conclusion, this invention has a very broad application prospect.

[0060] The above description of the disclosed embodiments enables those skilled in the art to make or use the invention. Various modifications to these embodiments will be readily 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 invention. Therefore, the invention is not to be limited to the embodiments shown herein, but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A rich-oil benzene removal column for separate distillation, comprising a column bottom (1), a column body (2), and a column top (3), characterized in that, One side of the tower body (2) is connected to a rich oil pipe (4) and a steam pipe (5), and the other side of the tower body (2) is connected to a naphthalene oil collection tank (6). A partition plate (7) for separation is installed inside the tower body (2). A liquid receiving plate and a downcomer are provided on both sides of the partition plate (7) to guide the liquid flow direction. The tower bottom (1) is connected to the tower body (2), and the tower bottom (1) is connected to a lean oil pipe (8). The tower top (3) is connected to a crude benzene pipe (9), and the crude benzene pipe (9) is connected to a reflux tank (10). The reflux tank (10) is connected to a reflux pipe (11). The reflux pipe (11) is connected to the crude benzene storage tank (12) and the inner cavity of the tower top (3). The inner cavity of the tower top (3) is connected to the tower body (2) through a liquid phase distribution pump (13). The tower body (2) includes a first tower body (201), a second tower body (202), and a third tower body (203) connected in sequence; the first tower body (201) is connected to the top of the tower (3), and the third tower body (203) is connected to the bottom of the tower (1). The partition plate (7) passes through the first tower body (201) and the second tower body (202) from top to bottom. The upper part of the first tower body (201) is provided with at least two liquid inlets (204). Each liquid inlet (204) is connected to the liquid outlet pipe of the liquid phase distribution pump (13). The liquid inlets (204) are evenly distributed on the left and right sides of the partition plate (7). The top of the tower (3) is provided with a gas outlet (301) connected to the crude benzene pipe (9). A condenser (40) connected to the reflux tank (10) is installed on the crude benzene pipe (9). A reflux inlet (302) connected to the reflux pipe (11) is provided on the outer wall of the tower (3). A liquid level gauge connection port (303) and a liquid outlet (304) are also provided on the outer wall of the tower (3). The liquid outlet (304) is connected to the liquid inlet pipe of the liquid phase distribution pump (13).

2. The rich-oil benzene removal tower for separated distillation according to claim 1, characterized in that, The projection of the partition plate (7) can be one of the following: straight line, broken line, arc, or any combination thereof; the interior of the first tower body (201), the second tower body (202), the third tower body (203), and the tower top (3) are uniformly equipped with multiple layers of tower plates from top to bottom.

3. The rich-oil benzene removal tower for separate distillation according to claim 1, characterized in that, The first tower body (201) is connected to multiple naphthalene oil pipelines (14) connected to the naphthalene oil collection tank (6), and a naphthalene oil extraction pump (15) is installed on the oil outlet pipeline of the naphthalene oil collection tank (6).

4. The rich-oil benzene removal tower for separate distillation according to claim 1, characterized in that, The top of the tower (3) is provided with a first tower plate (16) and a second tower plate (17). The first tower plate (16) and the second tower plate (17) are both provided with multiple layers and are evenly staggered in the upper and lower parts. A first liquid receiving tray (18) is provided on the left side of the first tower plate (16) and a first downcomer (19) is provided on the right side of the first tower plate (16). A second downcomer (20) is provided on the left side of the second tower plate (17) and a second liquid receiving tray (21) is provided on the right side of the second tower plate (17).

5. A rich-oil benzene removal tower for separated distillation according to claim 1, characterized in that, The first tower body (201) is provided with a third tower plate (22) and a fourth tower plate (23) symmetrically separated by a partition plate (7). The third tower plate (22) and the fourth tower plate (23) are provided with multiple layers and are evenly staggered vertically. The front end of the third tower plate (22) is provided with a third downcomer (24) and the rear end of the third tower plate (22) is provided with a third liquid receiving tray (25). The front end of the fourth tower plate (23) is provided with a fourth liquid receiving tray (26) and the rear end of the fourth tower plate (23) is provided with a fourth downcomer (27).

6. A rich-oil benzene removal tower for separate distillation according to claim 1, characterized in that, The interior of the second tower body (202) is provided with a fifth tower plate (28) and a sixth tower plate (29) symmetrically separated by a partition plate (7). The fifth tower plate (28) and the sixth tower plate (29) are each provided with multiple layers and are evenly staggered vertically. A fifth downcomer (30) is provided on the fifth tower plate (28) and the sixth tower plate (29). The fifth downcomer (30) is arranged on the left side of the partition plate (7). The upper part of the second tower body (202) is provided with a rich oil inlet (205) connected to the rich oil pipeline (4). The rich oil inlet (205) 205) Located above the fifth downcomer (30) at the top layer; the fifth receiving tray (31) is provided at the front left side of the fifth tray (28), the sixth downcomer (32) is provided at the front right side of the fifth tray (28), and the sixth receiving tray (33) is provided at the rear end of the fifth tray (28); the seventh downcomer (34) is provided at the front left side of the sixth tray (29), the seventh receiving tray (35) is provided at the front right side of the sixth tray (29), and the eighth downcomer (36) is provided at the rear end of the sixth tray (29).

7. A rich-oil benzene removal tower for separate distillation according to claim 1, characterized in that, The third tower body (203) is provided with a seventh tower plate (37) inside. The seventh tower plate (37) is provided with multiple layers. The seventh tower plate (37) is arranged vertically and alternately from top to bottom. A ninth downcomer (38) is provided on each of the seventh tower plates (37).

8. A rich-oil benzene removal tower for separate distillation according to claim 1, characterized in that, A reboiler (39) is provided on one side of the column bottom (1). The top port of the reboiler (39) is connected to the third column body (203), and the bottom port of the reboiler (39) is connected to the column bottom (1).

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