Heat exchange assembly for hydrogenation of diesel and wax oil, and hydrogenation system

Abstract

A heat exchange assembly for hydrogenation of diesel and wax oil, and a hydrogenation system. The heat exchange assembly comprises: a first heat exchanger, wherein an inlet of a first heat medium passage of the first heat exchanger is used for inputting a first-stage reaction effluent, an inlet of a first cold medium passage of the first heat exchanger is used for inputting a first-stage reaction influent, and an outlet of the first cold medium passage of the first heat exchanger is used for outputting the first-stage reaction influent having undergone heat exchange; a second heat exchanger, wherein an inlet of a second heat medium passage of the second heat exchanger is communicated with an outlet of the first heat medium passage, an outlet of the second heat medium passage of the second heat exchanger is used for being communicated with an inlet of a hot high-pressure separation tank, and an inlet of a second cold medium passage of the second heat exchanger is used for inputting a stripping tower bottom liquid; a third heat exchanger, wherein an inlet of a third heat medium passage of the third heat exchanger is used for inputting a second-stage reaction effluent, an inlet of a third cold medium passage of the third heat exchanger is communicated with an outlet of the second cold medium passage, and an outlet of the third cold medium passage of the third heat exchanger is used for being communicated with a downstream apparatus; and a fourth heat exchanger. Compared with the prior art, the present invention can reduce apparatus investment, and improve heat exchange efficiency.

Description

A heat exchange component and hydrogenation system for diesel wax oil hydrogenation Technical Field

[0001] The invention belongs to the technical field of petroleum processing, and in particular relates to a heat exchange component and a hydrogenation system for diesel wax oil hydrogenation. Background Art

[0002] The existing system for diesel wax oil hydrogenation is shown in Figure 1. It uses traditional shell-and-tube heat exchangers, which have a series of problems such as low heat exchange efficiency, easy internal leakage, and difficulty in large-scale equipment. A large heat exchange temperature difference is required, and the hot and cold logistics are cut into multiple temperature positions to achieve heat transfer design and equipment manufacturability. This results in a large number of heat exchange equipment units, many high-pressure pipelines and high-pressure sealing surfaces, a large area, and difficult piping work. The total investment, including device framework design and equipment cost, is large.

[0003] Summary of the Invention

[0004] The first technical problem to be solved by the present invention is to provide a heat exchange component for diesel wax oil hydrogenation in view of the current status of the existing technology, so as to reduce equipment investment and improve heat exchange efficiency.

[0005] The second technical problem to be solved by the present invention is to provide a hydrogenation system having the above-mentioned heat exchange component.

[0006] The technical solution adopted by the present invention to solve the above-mentioned first technical problem is: a heat exchange component for diesel wax oil hydrogenation, characterized in that it includes:

[0007] The first heat exchanger comprises a first hot medium channel and a first cold medium channel, wherein the inlet of the first hot medium channel is used for inputting a section of reaction effluent, the inlet of the first cold medium channel is used for inputting a section of reaction stream feed, and the outlet of the first cold medium channel is used for outputting a section of reaction stream feed after heat exchange;

[0008] The second heat exchanger has a second hot medium channel and a second cold medium channel. The inlet of the second hot medium channel is connected to the outlet of the first hot medium channel. The outlet of the second hot medium channel is used to connect to the inlet of the hot high separation tank. The inlet of the second cold medium channel is used to supply the stripping tower bottom liquid.

[0009] a third heat exchanger having a third hot medium channel and a third cold medium channel, wherein the inlet of the third hot medium channel is used for inputting the second-stage reaction effluent, the inlet of the third cold medium channel is connected to the outlet of the second cold medium channel, and the outlet of the third cold medium channel is used for connecting to a downstream device;

[0010] The fourth heat exchanger has a fourth hot medium channel and a fourth cold medium channel. The inlet of the fourth hot medium channel is connected to the outlet of the third heat medium channel. The outlet of the fourth hot medium channel is used to connect to the inlet of the hot high separation tank. The inlet of the fourth cold medium channel is used to supply the feed input of the second-stage reaction flow, and the outlet of the fourth cold medium channel is used to supply the feed output of the second-stage reaction flow after heat exchange.

[0011] The design and connection relationship of the four heat exchangers in the present invention can effectively increase the outlet temperature of the first-stage reaction flow feed and the second-stage reaction flow feed, thereby reducing the load of the subsequent high-pressure reaction heating furnace, that is, the investment in the high-pressure part of the heating furnace is reduced; and the present invention preferentially exchanges heat with the low-temperature and low-pressure stripping tower bottom liquid with the high-pressure reaction effluent, thereby expanding the heat transfer temperature difference of the heat exchanger in the high-pressure part and reducing the equipment investment in the heat exchanger in the high-pressure part; at the same time, the second-stage reaction effluent is first heat-exchanged with the stripping tower bottom liquid, which helps to increase the temperature of the stripping tower bottom liquid; in summary, the present invention reduces the number of heat exchanger equipment while improving the heat exchange efficiency, so that the system occupies less space, is convenient for piping, and has a significantly reduced total investment.

[0012] In order to facilitate adjustment according to actual working conditions, preferably, the inlet of the first cold medium channel of the first heat exchanger is connected to a first feed pipeline for conveying a section of the reaction flow feed, and the first feed pipeline is provided with a first feed valve for controlling the flow rate, and the outlet of the first cold medium channel is connected to a first discharge pipeline for conveying the section of the reaction flow feed after heat exchange;

[0013] It also includes a first bypass line and a first bypass valve provided on the first bypass line for controlling flow, the inlet end of the first bypass line is connected to the first feed line, and the outlet end of the first bypass line is connected to the first discharge line.

[0014] Preferably, the first feed pipeline includes a raw oil pipeline for transporting raw oil and a hydrogen pipeline for transporting hydrogen, and the outlet of the raw oil pipeline and the outlet of the hydrogen pipeline are both connected to the inlet of the first cold medium channel of the first heat exchanger;

[0015] The inlet end of the first bypass pipeline is connected to the raw oil pipeline, and the first feed valve is provided on the raw oil pipeline.

[0016] Preferably, the inlet of the second cold medium channel of the second heat exchanger is connected to a second feed pipeline for conveying the stripping tower bottom liquid, and the second feed pipeline is provided with a second feed valve for controlling the flow rate, and the outlet of the second cold medium channel is connected to the inlet of the third cold medium channel of the third heat exchanger via a second discharge pipeline;

[0017] It also includes a second bypass line and a second bypass valve provided on the second bypass line for controlling flow, the inlet end of the second bypass line is connected to the second feed line, and the outlet end of the second bypass line is connected to the second discharge line.

[0018] Preferably, the outlet of the third cold medium channel of the third heat exchanger is connected to a third discharge pipeline;

[0019] It also includes a third bypass pipeline and a third bypass valve for controlling flow rate, the inlet end of the third bypass pipeline is connected to the second discharge pipeline, and the outlet end of the second bypass pipeline is connected to the third discharge pipeline; and a third feed valve for controlling flow rate is provided on the second discharge pipeline at a position between the inlet end of the third bypass pipeline and the inlet of the third cold medium channel.

[0020] In the above solution, preferably, the inlet of the second cold medium channel of the second heat exchanger is connected to a second feed pipeline for conveying the stripping tower bottom liquid, and the second feed pipeline is provided with a second feed valve for controlling the flow rate; the outlet of the third cold medium channel of the third heat exchanger is connected to a third discharge pipeline;

[0021] It also includes a large bypass pipeline and a large bypass valve arranged on the large bypass pipeline for controlling flow, the inlet end of the large bypass pipeline is connected to the second feed pipeline, and the outlet end of the large bypass pipeline is connected to the third discharge pipeline.

[0022] In the aforementioned heat exchange components, the stripping tower bottoms liquid or crude oil serves as the cold fluid, flowing through the heat exchanger's cold medium channel and bypass pipeline. However, the design of the bypass pipeline and bypass valve must take into account factors such as the on-site framework and pipe corridor. Bypass pipelines are often long, with large bypass level differences, resulting in a bypass pressure drop greater than the pressure drop of the fluid flowing through the heat exchange equipment. This makes it impossible to properly regulate the bypass pipeline, causing the temperature of the cold fluid after heat exchange to be higher than the designed value, affecting the subsequent heat exchange network and operation. At the same time, if the temperature of the cold fluid after heat exchange is too high, exceeding the maximum temperature that the pipeline can withstand, it will cause pipeline leakage or even explosion, posing a safety hazard.

[0023] Therefore, in each of the above solutions, to improve operational safety, preferably, at least one of the first, second, and third bypass lines is disposed within the corresponding heat exchanger to form a bypass channel, with the outlet of the bypass channel communicating with the outlet of the cold medium channel within the corresponding heat exchanger. This allows the bypass medium to mix with the post-heat exchange cold fluid before being output, and the resulting mixed medium can be lower in temperature than the post-heat exchange cold fluid, thereby resolving the safety issue of the post-heat exchange cold fluid being too hot.

[0024] Preferably, the heat exchanger is a wound tube heat exchanger, comprising a shell and the above-mentioned cold medium channel as a shell side or a tube side, the shell being provided with a cold medium inlet pipe connected to the inlet end of the cold medium channel, a cold medium outlet pipe connected to the outlet end of the cold medium channel, and a bypass medium inlet pipe connected to the inlet end of the bypass channel; the outlet end of the bypass channel is connected to the outlet end of the cold medium channel, and the cold medium outlet pipe is used to output a mixed medium after the cold medium and the bypass medium are mixed.

[0025] Furthermore, an extension direction of the bypass channel is consistent with an extension direction of the cold medium channel, and an inlet end of the bypass channel is relatively close to an inlet end of the cold medium channel.

[0026] Furthermore, the bypass channel is located in the cold medium channel.

[0027] In order to improve the compactness of the structure, preferably, the bypass channel extends up and down and is arranged in the center of the shell as a central tube; the heat exchange tubes in the tube pass are spirally wound around the outer circumference of the bypass channel.

[0028] In the above solution, in order to prevent the medium from flowing back in the bypass channel while not affecting the normal transportation of the bypass medium, preferably, a switch component that can cut off or open the passage in the bypass channel is provided near the outlet end of the bypass channel.

[0029] Preferably, the switch element includes a valve plate and an elastic member, and the valve plate is rotatably arranged in the bypass channel to cut off or open the passage in the bypass channel; the elastic member acts on the valve plate so that the valve plate always has a tendency to rotate to cut off the passage; at the same time, under the action of the bypass medium flowing from the inlet end to the outlet end in the bypass channel, the valve plate is arranged to overcome the elastic force of the elastic member and rotate to a state of opening the passage.

[0030] In this way, the valve plate can prevent the bypass medium from flowing back into the bypass, and when the bypass medium flows normally in the bypass, the bypass medium can break through the valve plate and open the passage, thereby not affecting the normal transportation of the bypass medium.

[0031] Preferably, a door plate with a through hole is placed horizontally in the bypass channel, and the valve plate is rotatably provided on the door plate. The valve plate is located downstream of the door plate along the flow direction of the bypass medium from the inlet end to the outlet end of the bypass channel to open and close the through hole. When the valve plate opens the through hole, the passage in the bypass channel is connected, and when the valve plate closes the through hole, the passage in the bypass channel is cut off.

[0032] Furthermore, the edge of one side of the valve plate is rotatably connected to the door plate via a rotating shaft, and the elastic member is a torsion spring sleeved on the outer periphery of the rotating shaft.

[0033] Furthermore, the shell is provided with two tube sheets for supporting the upper and lower ends of the heat exchange tubes, and at least one end of the bypass channel is constrained to the tube sheet in a manner that it can move telescopically up and down relative to the corresponding tube sheet.

[0034] The technical solution adopted by the present invention to solve the above-mentioned second technical problem is: a hydrogenation system, comprising a distillation tower, a stripping tower, a heating furnace, a hot high separation tank and a first heat exchange device, characterized in that it also has the heat exchange component as described above, the inlet of the second cold medium channel of the second heat exchanger is connected to the outlet at the bottom of the stripping tower, the inlet of the hot high separation tank is connected to the outlet of the second hot medium channel of the second heat exchanger and the outlet of the fourth hot medium channel of the fourth heat exchanger, the outlet at the top of the hot high separation tank is connected to the inlet of the hot medium channel of the first heat exchange device, the inlet of the cold medium heat exchange channel of the first heat exchange device is connected to a stripping tower feed pipeline for conveying stripping tower feed, and the outlet of the cold medium heat exchange channel of the first heat exchange device is connected to the feed port of the stripping tower;

[0035] The outlet of the third cold medium channel of the third heat exchanger is connected to the input end of the heating furnace, and the output end of the heating furnace is connected to the feed inlet of the distillation tower.

[0036] Preferably, a second heat exchange device is further included, wherein the inlet of its cold medium heat exchange channel is connected to the outlet of the third cold medium channel of the third heat exchanger, the outlet of its cold medium heat exchange channel is connected to the input end of the heating furnace, and the inlet of its hot medium heat exchange channel is connected to the outlet at the bottom of the fractionating tower. In this way, the unconverted oil at the bottom of the fractionating tower can be used to heat the bottom liquid of the stripping tower, reducing the load on the heating furnace before the fractionating tower is fed.

[0037] Furthermore, a third heat exchange device is included, the inlet of the hot medium heat exchange channel of which is connected to the outlet of the hot medium heat exchange channel of the second heat exchange device, and the inlet of the cold medium heat exchange channel of which is connected to a water supply pipeline for conveying water.

[0038] Furthermore, the first heat exchange device has three cold medium heat exchange channels. The inlet of the first cold medium heat exchange channel is connected to a hydrogen supply pipeline for transporting hydrogen, the inlet of the second cold medium heat exchange channel is connected to the aforementioned stripping tower feed pipeline, and the inlet of the third cold medium heat exchange channel is connected to a water supply pipeline for transporting water. The first, second, and third cold medium heat exchange channels are arranged sequentially along the flow direction of the hot high-fraction gas within the hot medium channel of the first heat exchange device. In this way, the heat of the hot high-fraction gas can be fully utilized.

[0039] Compared with the prior art, the advantages of the present invention are: the design and connection relationship of the four heat exchangers in the present invention can effectively increase the outlet temperature of the first-stage reaction flow feed and the second-stage reaction flow feed, thereby reducing the load of the subsequent high-pressure reaction heating furnace, that is, the investment in the heating furnace of the high-pressure part is reduced; and the present invention preferentially exchanges heat with the low-temperature and low-pressure stripping tower bottom liquid with the high-pressure reaction effluent, thereby expanding the heat transfer temperature difference of the heat exchanger of the high-pressure part and reducing the equipment investment of the heat exchanger of the high-pressure part; at the same time, the second-stage reaction effluent is first heat-exchanged with the stripping tower bottom liquid, which helps to increase the temperature of the stripping tower bottom liquid; in summary, the present invention reduces the number of heat exchanger equipment while improving the heat exchange efficiency, so that the system occupies less space, is convenient for piping, and has a significantly reduced total investment. BRIEF DESCRIPTION OF THE DRAWINGS

[0040] FIG1 is a schematic structural diagram of a hydrogenation system in the prior art;

[0041] FIG2 is a schematic structural diagram of a hydrogenation system in Example 1 of the present invention;

[0042] FIG3 is a schematic structural diagram of a heat exchange assembly in a second embodiment of the present invention (corresponding to the portion within the dotted box in FIG2 );

[0043] FIG4 is a schematic structural diagram of a heat exchange assembly in a third embodiment of the present invention (corresponding to the portion within the dotted box in FIG2 );

[0044] FIG5 is a schematic structural diagram of a heat exchange assembly in a fourth embodiment of the present invention (corresponding to the portion within the dotted box in FIG2 );

[0045] FIG6 is a schematic structural diagram of a heat exchanger in a fourth embodiment of the present invention;

[0046] Structural diagram;

[0047] FIG7 is a schematic structural diagram of a heat exchanger in Embodiment 5 of the present invention;

[0048] FIG8 is a schematic structural diagram of a heat exchanger in Example 6 of the present invention;

[0049] FIG9 is an enlarged view of portion A in FIG8 ;

[0050] FIG10 is a cross-sectional view of portion A in FIG8 . DETAILED DESCRIPTION

[0051] The present invention will be described in further detail below with reference to the accompanying drawings and embodiments.

[0052] Example 1:

[0053] As shown in FIG2 , a preferred embodiment of a heat exchange component and a hydrogenation system for hydrogenating diesel wax oil according to the present invention is shown. The hydrogenation system includes a heat exchange component, a distillation tower 200, a stripping tower 300, a heating furnace 400, a hot high separation tank 500, and a first heat exchange device 600, a second heat exchange device 700, and a third heat exchange device 800.

[0054] The heat exchange assembly includes a first heat exchanger 110 , a second heat exchanger 120 , a third heat exchanger 130 , and a fourth heat exchanger 140 .

[0055] The first heat exchanger 110 has a first hot medium channel and a first cold medium channel. The inlet of the first hot medium channel is used to supply a section of reaction effluent, the inlet of the first cold medium channel is used to supply a section of reaction flow feed, the outlet of the first cold medium channel is used to supply a section of reaction flow feed after heat exchange, and the outlet of the first cold medium channel is used to connect to a reverse feed heating furnace.

[0056] The second heat exchanger 120 has a second hot medium channel and a second cold medium channel. The inlet of the second hot medium channel is connected to the outlet of the first hot medium channel of the first heat exchanger 110, and the outlet of the second hot medium channel is connected to the inlet of the hot high separation tank 500; the inlet of the second cold medium channel is connected to the outlet at the bottom of the stripping tower 300.

[0057] The third heat exchanger 130 has a third hot medium channel and a third cold medium channel. The inlet of the third hot medium channel is used for inputting the second-stage reaction effluent, and the inlet of the third cold medium channel is connected to the outlet of the second cold medium channel of the second heat exchanger 120.

[0058] The fourth heat exchanger 140 has a fourth hot medium channel and a fourth cold medium channel. The inlet of the fourth hot medium channel is connected to the outlet of the third hot medium channel of the third heat exchanger 130. The outlet of the fourth hot medium channel is connected to the inlet of the hot high separation tank 500. The inlet of the fourth cold medium channel is used for feeding the second-stage reaction flow, and the outlet of the fourth cold medium channel is used for feeding the second-stage reaction flow after heat exchange. The outlet of the fourth cold medium channel is used to be connected to the second reverse feed heating furnace.

[0059] The first heat exchange device 600 has one hot medium channel and three cold medium heat exchange channels. The inlet of the hot medium channel of the first heat exchange device 600 is connected to the outlet at the top of the hot high separation tank 500, and the outlet of the hot medium channel of the first heat exchange device 600 is connected to the downstream air cooler. The inlet of the first of the three cold medium heat exchange channels is connected to a hydrogen supply pipeline 610 for transporting hydrogen, the inlet of the second cold medium heat exchange channel is connected to a stripping tower feed pipeline 310 for transporting stripping tower feed, and the inlet of the third cold medium heat exchange channel is connected to a water supply pipeline 620 for transporting water. The first, second, and third cold medium heat exchange channels are arranged sequentially along the flow direction of the hot high separation gas within the hot medium channel of the first heat exchange device 600.

[0060] The stripping tower 300 is a desulfurization stripping tower, and its feed port is connected to the outlet of the second cold medium heat exchange channel of the first heat exchange device 600. The stripping tower 300 has a steam inlet at its lower portion.

[0061] The outlet of the third cold medium channel of the third heat exchanger 130 is connected to the feed port of the fractionating tower 200 in sequence through the second heat exchange device 700 and the heating furnace 400. Specifically, the inlet of the cold medium heat exchange channel of the second heat exchange device 700 is connected to the outlet of the third cold medium channel of the third heat exchanger 130, the outlet of the cold medium heat exchange channel of the second heat exchange device 700 is connected to the input end of the heating furnace 400, the output end of the heating furnace 400 is connected to the feed port of the fractionating tower 200, and the inlet of the hot medium heat exchange channel of the second heat exchange device 700 is connected to the outlet at the bottom of the fractionating tower 200.

[0062] The inlet of the hot medium heat exchange channel of the third heat exchange device 800 is connected to the outlet of the hot medium heat exchange channel of the second heat exchange device 700, and the inlet of the cold medium heat exchange channel is connected to a water supply pipeline 810 for conveying water.

[0063] The heat exchange process of this embodiment is as follows:

[0064] The first stage reaction effluent passes through the first heat medium channel of the first heat exchanger 110 and the second heat medium channel of the second heat exchanger 120 in sequence and is then fed into the hot high separation tank 500. The temperature of the first stage reaction effluent before entering the first heat medium channel of the first heat exchanger 110 is 425° C. and the pressure is 17.08 MPa. The temperature of the first stage reaction effluent output from the second heat medium channel of the second heat exchanger 120 is 255° C. At the same time, a first stage reaction stream feed (temperature of 207° C. and pressure of 19.54 MPa) is fed into the first cold medium channel of the first heat exchanger 110 to exchange heat with the first stage reaction effluent. After heat exchange, the first stage reaction stream feed (temperature of 405° C.) is fed into a reverse feed heating furnace.

[0065] The second-stage reaction effluent passes through the third heat medium channel of the third heat exchanger 130 and the fourth heat medium channel of the fourth heat exchanger 140 in sequence and is then input into the hot high separation tank 500. The temperature of the second-stage reaction effluent before entering the third heat medium channel of the third heat exchanger 130 is 403° C. and the pressure is 16.8 MPa. The temperature of the second-stage reaction effluent output from the fourth heat medium channel of the fourth heat exchanger 140 is 255° C. At the same time, the second-stage reaction flow feed (temperature of 216° C. and pressure of 18.3 MPa) is input into the fourth cold medium channel of the fourth heat exchanger 140 to exchange heat with the second-stage reaction effluent. After heat exchange, the second-stage reaction flow feed (temperature of 380° C.) is sent to the second reactor feed heating furnace.

[0066] The hot high fraction gas (pressure of 16.4 MPa) output from the top of the hot high separation tank 500 passes through the heat medium channel of the first heat exchange device 600 and is output to the air cooler. The temperature of the hot high fraction gas output from the heat medium channel of the first heat exchange device 600 is 90°C. At the same time, hydrogen enters the first cold medium heat exchange channel of the first heat exchange device 600 through the hydrogen supply pipeline 610 to perform heat exchange with the hot high fraction gas. The temperature of the hydrogen before the heat exchange is 87°C and the temperature of the hydrogen after the heat exchange is 20 0.7°C; the stripping tower feed enters the second cold medium heat exchange channel of the first heat exchange device 600 through the stripping tower feed pipeline 310 to exchange heat with the hot high-fraction gas, and the temperature of the stripping tower feed before the heat exchange is 49°C, and the temperature of the stripping tower feed after the heat exchange is 166.6°C; water enters the third cold medium heat exchange channel of the first heat exchange device 600 through the water supply pipeline 620 to exchange heat with the hot high-fraction gas, and the water temperature before the heat exchange is 70°C, and the water temperature after the heat exchange is 95°C;

[0067] The stripping tower bottom liquid output from the bottom of the stripping tower passes through the second cold medium channel of the second heat exchanger 120, the third cold medium channel of the third heat exchanger 130, the cold medium heat exchange channel of the second heat exchange device 700, and the heating furnace 400 in sequence, and is then input into the fractionation tower 200. The stripping tower bottom liquid output from the bottom of the stripping tower has a temperature of 213° C. and a pressure of 3.0 MPa. The stripping tower bottom liquid output from the second cold medium channel of the second heat exchanger 120 has a temperature of 276° C., the stripping tower bottom liquid output from the third cold medium channel of the third heat exchanger 130 has a temperature of 282.4° C., and the stripping tower bottom liquid output from the cold medium heat exchange channel of the second heat exchange device 700 has a temperature of 307.5° C.

[0068] At the same time, the unconverted oil output from the bottom of the fractionating tower passes through the heat medium heat exchange channel of the second heat exchange device 700 and the heat medium heat exchange channel of the third heat exchange device 800 before being output. The unconverted oil output from the bottom of the fractionating tower has a temperature of 354°C and a pressure of 1.6 MPa. The unconverted oil output from the heat medium heat exchange channel of the second heat exchange device 700 has a temperature of 287.5°C, and the unconverted oil output from the heat medium heat exchange channel of the third heat exchange device 800 has a temperature of 240°C. Simultaneously, 70°C water enters the cold medium channel of the third heat exchange device 800 through the water supply line 810, exchanges heat with the unconverted oil, and is output at a temperature of 95°C.

[0069] This embodiment effectively increases the outlet temperature of the first-stage reaction flow feed and the second-stage reaction flow feed, thereby reducing the load of the subsequent high-pressure reaction heating furnace, that is, reducing the investment in the high-pressure part of the heating furnace.

[0070] A 10-15°C temperature rise is reserved for the reaction feed heating furnace, facilitating adjustments to operating conditions. Combined with a large bypass for the crude oil and stripping tower bottoms, the entire system is more convenient and efficient to adjust.

[0071] Compared with the prior art, the design load of the low-pressure heating furnace 400 in this embodiment needs to be increased, but due to the low pressure, the cost increase ratio is not large.

[0072] In addition, in this embodiment, the heat exchange between the hot high-fraction gas and the stripping tower feed can increase the stripping tower feed temperature, thereby effectively reducing the steam consumption of the stripping tower.

[0073] By designing the second heat exchange device 700, the heat exchange temperature difference between the unconverted oil and the stripping tower bottom liquid is reduced, and the load of the heating furnace 400 before the fractionation tower is fed can be reduced.

[0074] The first to fourth heat exchangers are all wound tube heat exchangers.

[0075] Example 2:

[0076] As shown in FIG3 , a preferred embodiment 2 of a heat exchange assembly and hydrogenation system for diesel wax oil hydrogenation according to the present invention is shown. This embodiment is substantially the same as the first embodiment, except that in this embodiment, the inlet of the second cold medium channel of the second heat exchanger 120 is connected to a second feed pipeline 121 for conveying the stripping tower bottom liquid, and the second feed pipeline 121 is provided with a second feed valve 122 for controlling the flow rate. The outlet of the second cold medium channel is connected to the inlet of the third cold medium channel of the third heat exchanger 130 via a second discharge pipeline 123; and the outlet of the third cold medium channel of the third heat exchanger 130 is connected to a third discharge pipeline 133.

[0077] It also includes a second bypass pipeline 124 and a second bypass valve 125 arranged on the second bypass pipeline 124 for controlling the flow rate. The inlet end of the second bypass pipeline 124 is connected to the second feed pipeline 121, and the outlet end of the second bypass pipeline 124 is connected to the second discharge pipeline 123 near the outlet of the second cold medium channel of the second heat exchanger 120.

[0078] It also includes a third bypass pipeline 134 and a third bypass valve 135 for controlling the flow rate, the inlet end of the third bypass pipeline 134 is connected to the second discharge pipeline 123 near the inlet of the third cold medium channel of the third heat exchanger 130, and the outlet end of the second bypass pipeline 124 is connected to the third discharge pipeline 133; and a third feed valve 132 for controlling the flow rate is provided on the second discharge pipeline 123 between the inlet end of the third bypass pipeline 134 and the inlet of the third cold medium channel.

[0079] The provision of each bypass pipeline in this embodiment facilitates the adjustment of the temperature of the medium in the corresponding discharge pipeline.

[0080] Example 3:

[0081] As shown in FIG4 , a preferred embodiment 3 of a heat exchange assembly and hydrogenation system for diesel wax oil hydrogenation of the present invention is shown. This embodiment is substantially the same as the first embodiment, except that in this embodiment, the outlet of the first cold medium channel of the first heat exchanger 110 is connected to a first discharge pipeline 113 for conveying a section of the reaction stream after heat exchange; the inlet of the first cold medium channel of the first heat exchanger 110 is connected to a first feed pipeline 111 for conveying a section of the reaction stream, the first feed pipeline 111 includes a raw oil pipeline 1111 for conveying raw oil and a hydrogen pipeline 1112 for conveying hydrogen, the outlet of the raw oil pipeline 1111 and the outlet of the hydrogen pipeline 1112 are both connected to the inlet of the first cold medium channel of the first heat exchanger 110, and the raw oil pipeline 1111 is provided with a first feed valve 112 for controlling the flow rate;

[0082] It also includes a first bypass pipeline 114 and a first bypass valve 115 arranged on the first bypass pipeline 114 for controlling the flow rate. The inlet end of the first bypass pipeline 114 is connected to the crude oil pipeline 1111, and the outlet end of the first bypass pipeline 114 is connected to the first discharge pipeline 113.

[0083] At the same time, the inlet of the second cold medium channel of the second heat exchanger 120 is connected to a second feed pipeline 121 for conveying the stripping tower bottom liquid, and the second feed pipeline 121 is provided with a second feed valve 122 for controlling the flow rate; the outlet of the third cold medium channel of the third heat exchanger 130 is connected to a third discharge pipeline 133;

[0084] It also includes a large bypass pipeline 144 and a large bypass valve 145 provided on the large bypass pipeline 144 for controlling the flow rate. The inlet end of the large bypass pipeline 144 is connected to the second feed pipeline 121, and the outlet end of the large bypass pipeline 144 is connected to the third discharge pipeline 133.

[0085] Likewise, the provision of each bypass pipeline in this embodiment facilitates the adjustment of the temperature of the medium in the corresponding discharge pipeline.

[0086] Example 4:

[0087] As shown in Figures 5 and 6, a fourth preferred embodiment of a heat exchange assembly and hydrogenation system for diesel wax oil hydrogenation of the present invention is shown. This embodiment is basically the same as the second embodiment, except that in this embodiment, the outlet of the first cold medium channel of the first heat exchanger 110 is connected to a first discharge pipeline 113 for conveying a section of the reaction stream after heat exchange; the inlet of the first cold medium channel of the first heat exchanger 110 is connected to a first feed pipeline 111 for conveying a section of the reaction stream, and the first feed pipeline 111 includes a raw oil pipeline 1111 for conveying raw oil and a hydrogen pipeline 1112 for conveying hydrogen. The outlet of the raw oil pipeline 1111 and the outlet of the hydrogen pipeline 1112 are both connected to the inlet of the first cold medium channel of the first heat exchanger 110, and the raw oil pipeline 1111 is provided with a first feed valve 112 for controlling the flow rate (not shown in Figure 5, see Figure 4);

[0088] It also includes a first bypass pipeline 114 and a first bypass valve 115 arranged on the first bypass pipeline 114 for controlling the flow rate. The inlet end of the first bypass pipeline 114 is connected to the crude oil pipeline 1111, and the outlet end of the first bypass pipeline 114 is connected to the first discharge pipeline 113.

[0089] At the same time, in this embodiment, the first bypass line 114, the second bypass line 124, and the third bypass line 134 are respectively provided in their corresponding heat exchangers to form three bypass channels 2 (see FIG6 ), and the outlet of each bypass channel 2 is connected to the outlet of the cold medium channel in the corresponding heat exchanger. Specifically:

[0090] As shown in FIG6 , each heat exchanger is a wound tube heat exchanger and includes a shell 1 , a bypass channel 2 and a heat exchange tube 3 .

[0091] The shell 1 is a vertically arranged cylindrical structure, with a cooling medium inlet pipe 100a and a cooling medium outlet pipe 100b respectively provided at the upper and lower ends of the shell 1. Furthermore, a shell-side inlet pipe 1a for the input of the heating medium is provided at the lower portion of the side wall of the shell 1, and a shell-side outlet pipe 1b for the output of the heating medium is provided at the upper portion of the side wall of the shell 1. The shell-side inlet pipe 1a and the shell-side outlet pipe 1b communicate with the interior of the shell 1 (the shell 101 serving as the heat exchanger).

[0092] The bypass channel 2 extends vertically and serves as a central tube within the center of the housing 1. Tube sheets 5 are located at each end of the bypass channel 2 within the housing 1. The lower end of the bypass channel 2 is located above the corresponding tube sheet 5, and the two are fixed to each other. The lower end of the bypass channel 2 is connected to the cold medium outlet pipe 100b. The upper end of the bypass channel 2 is located below the corresponding tube sheet 5, and the two are plugged together, allowing the upper end of the bypass channel 2 to move up and down relative to the tube sheet 5. The upper end of the bypass channel 2 is also connected to the cold medium inlet pipe 100a.

[0093] The above-mentioned heat exchange tube 3 is wound around the outer periphery of the bypass channel 2 as the tube side 102 (i.e., the cold medium channel) of the heat exchanger. The upper and lower ends of the heat exchange tube 3 are respectively supported on the corresponding tube sheets 5 and are respectively connected to the corresponding cold medium inlet pipe 100a and cold medium outlet pipe 100b.

[0094] At the same time, a bypass medium inlet pipe 2a is provided at the upper portion of the shell 1, relatively close to the cold medium inlet pipe 100a. A portion of the bypass medium inlet pipe 2a extends downward through the corresponding tube sheet 5 and into the upper port of the bypass channel 2 (serving as the inlet end of the bypass channel 2), communicating with the bypass channel 2. The lower port of the bypass channel 2 (serving as the outlet end of the bypass channel 2) is connected to the lower port of the heat exchange tube 3. The cold medium outlet pipe 100b is used to output the mixed medium of the cold medium and the bypass medium.

[0095] During operation, hot medium enters shell 1 through shell-side inlet pipe 1a, exchanges heat with cold medium, and exits through shell-side outlet pipe 1b. Bypass medium enters bypass channel 2 through bypass medium inlet pipe 2a. Cold medium enters heat exchange tube 3 through cold medium inlet pipe 100a, exchanges heat with hot medium, flows out of heat exchange tube 3, and mixes with the bypass medium before exiting through cold medium outlet pipe 100b.

[0096] Likewise, the provision of each bypass pipeline in this embodiment facilitates the adjustment of the temperature of the medium in the corresponding discharge pipeline.

[0097] Embodiment 5:

[0098] As shown in FIG7 , a fifth preferred embodiment of a heat exchange assembly and a hydrogenation system for diesel wax oil hydrogenation according to the present invention is shown. This embodiment is substantially the same as the fourth embodiment, except that:

[0099] Shell 1 is a vertically mounted cylindrical structure, with a cooling medium outlet pipe 100b and a cooling medium inlet pipe 100a provided at the upper and lower ends, respectively. A shell-side inlet pipe 1a for heating medium input is provided at the upper side of the shell 1, while a shell-side outlet pipe 1b for heating medium output is provided at the lower side of the shell 1. Both shell-side inlet pipe 1a and shell-side outlet pipe 1b communicate with the interior of the shell 1 (shell 101, which serves as the heat exchanger).

[0100] The bypass channel 2 extends vertically and serves as a central tube located in the center of the housing 1. Tube sheets 5 are located at each end of the bypass channel 2 within the housing 1. The lower end of the bypass channel 2 is located above the corresponding tube sheet 5, and the two are fixed to each other. The upper end of the bypass channel 2 is located below the corresponding tube sheet 5, and the two are plugged together, allowing the upper end of the bypass channel 2 to move up and down relative to the tube sheet 5. The upper end of the bypass channel 2 is connected to the cold medium outlet pipe 100b.

[0101] The above-mentioned heat exchange tube 3 is wound around the outer circumference of the bypass channel 2 as the tube side 102 (i.e., the cold medium channel) of the heat exchanger. The upper and lower ends of the heat exchange tube 3 are respectively supported on the corresponding tube sheets 5 and are respectively connected to the corresponding cold medium outlet pipe 100b and cold medium inlet pipe 100a.

[0102] At the same time, a bypass medium inlet pipe 2a is provided at the lower portion of the shell 1, relatively close to the cold medium inlet pipe 100a. A portion of the bypass medium inlet pipe 2a extends upward through the corresponding tube sheet 5 and into the lower port of the bypass channel 2 (serving as the inlet end of the bypass channel 2), communicating with the bypass channel 2. The upper port of the bypass channel 2 (serving as the outlet end of the bypass channel 2) is connected to the upper port of the heat exchange tube 3. The cold medium outlet pipe 100b is used to output the mixed medium formed by mixing the tube-side medium and the bypass medium.

[0103] During operation, hot medium enters shell 1 through shell-side inlet pipe 1a, exchanges heat with cold medium, and exits through shell-side outlet pipe 1b. Bypass medium enters bypass channel 2 through bypass medium inlet pipe 2a. Cold medium enters heat exchange tube 3 through cold medium inlet pipe 100a, exchanges heat with hot medium, flows out of heat exchange tube 3, and mixes with the bypass medium before exiting through cold medium outlet pipe 100b.

[0104] Example 6:

[0105] As shown in Figures 8 to 10, a sixth preferred embodiment of a heat exchange assembly and hydrogenation system for diesel wax oil hydrogenation according to the present invention is shown. This embodiment is substantially the same as the fourth embodiment, except that:

[0106] The wound tube heat exchanger includes a shell 1, a bypass channel 2, a switch component and a heat exchange tube 3.

[0107] The shell 1 is a vertically arranged cylindrical structure, with a pipe-side inlet pipe for inputting the pipe-side medium and a pipe-side outlet pipe for outputting the pipe-side medium, respectively, located at the upper and lower ends of the shell 1. Furthermore, a cold medium inlet pipe 100a for inputting the cooling medium is located at the lower portion of the side wall of the shell 1, while a cold medium outlet pipe 100b for outputting the cooling medium is located at the upper portion of the side wall of the shell 1. The cold medium inlet pipe 100a and the cold medium outlet pipe 100b communicate with the interior of the shell 1 (serving as the shell side 101 of the heat exchanger, i.e., the cold medium passage).

[0108] The bypass channel 2 extends vertically and serves as a central tube located in the center of the housing 1. Tube sheets 5 are located at each end of the housing 1, corresponding to the bypass channel 2. The lower end of the bypass channel 2 (serving as the inlet) is located above the corresponding tube sheet 5, and the two are fixed to each other. The upper end of the bypass channel 2 (serving as the outlet) is located below the corresponding tube sheet 5, and the two are plugged together, allowing the upper end of the bypass channel 2 to move up and down relative to the tube sheet 5.

[0109] The heat exchange tube 3 is wound around the outer periphery of the bypass channel 2 as the tube side 102 of the heat exchanger. The upper and lower ends of the heat exchange tube 3 are respectively supported on the corresponding tube sheets 5 and are respectively connected to the corresponding tube side inlet pipe and tube side outlet pipe.

[0110] At the same time, a bypass medium inlet pipe 2a is provided at the lower portion of the side wall of the housing 1, corresponding to the lower end of the bypass channel 2. A portion of the bypass medium inlet pipe 2a extends laterally into the housing 1 and communicates with the bypass channel 2. A fluid outlet 22 is provided at the upper end of the bypass channel 2 (serving as the outlet of the bypass channel 2). This fluid outlet 22 opposes the cold medium outlet pipe 100b, and the two are connected through the interior space of the housing 1. In other words, the cold medium outlet pipe 100b is used to output a mixed medium formed by mixing the cold medium and the bypass medium.

[0111] During operation, the hot medium is input into the heat exchange tube 3 from the tube inlet pipe, exchanges heat with the cold medium and flows out of the heat exchange tube 3. The bypass medium is input into the bypass channel 2 from the bypass medium inlet pipe 2a. The cold medium is input into the shell 1 from the cold medium inlet pipe 100a. After exchanging heat with the hot medium, it is mixed with the bypass medium and output from the cold medium outlet pipe 100b.

[0112] The switch element is located within the bypass channel 2, near the upper end of the bypass channel 2 and below the fluid outlet 22. Specifically, a door plate 25 with a through hole 250 is positioned horizontally within the bypass channel 2, corresponding to the switch element. The switch element comprises a valve disc 23 and an elastic member 24. One edge of the valve disc 23 is pivotally connected to the door plate 25 via a rotating shaft 231 to open and close the through hole 250. When the valve disc 23 opens the through hole 250, the bypass channel 2 is open; when the valve disc 23 closes the through hole 250, the bypass channel 2 is closed. The elastic member 24 is a torsion spring mounted around the outer periphery of the rotating shaft 231, ensuring that the valve disc 23 always has a tendency to rotate to close the through hole 250. Furthermore, under the action of the bypass medium flowing upward from bottom to top within the bypass channel 2, the valve disc 23 is configured to overcome the elastic force of the elastic member 24 and rotate to an open position. In this way, the valve plate 23 can only open the through hole 250 under the action of the bypass medium flowing from bottom to top, thereby making the passage in the bypass channel 2 conductive.

[0113] In the present specification and claims, directional terms such as "front," "back," "up," "down," "left," "right," "side," "top," and "bottom" are used to describe various exemplary structural parts and components of the present invention. However, these terms are used herein for convenience of description only and are based on the exemplary orientations shown in the accompanying drawings. Because the embodiments disclosed herein can be arranged in various orientations, these directional terms are intended for illustrative purposes only and should not be construed as limiting. For example, "up" and "down" are not necessarily limited to directions opposite to or consistent with the direction of gravity.

[0114] The term "vertical" is also used in the specification and claims of the present invention, which means basically along the up and down direction, and is not limited to the vertical direction, and can also be slightly deviated from the vertical direction.

Claims

1. A heat exchange component for hydrogenation of diesel oil, characterized in that Included are: A first heat exchanger (110) has a first hot medium channel and a first cold medium channel, wherein the inlet of the first hot medium channel is used for inputting a section of reaction effluent, the inlet of the first cold medium channel is used for inputting a section of reaction flow feed, and the outlet of the first cold medium channel is used for outputting a section of reaction flow feed after heat exchange; The second heat exchanger (120) has a second hot medium channel and a second cold medium channel, wherein the inlet of the second hot medium channel is connected to the outlet of the first hot medium channel, and the outlet of the second hot medium channel is used to be connected to the inlet of the hot high separation tank (500); the inlet of the second cold medium channel is used to supply the stripping tower bottom liquid; A third heat exchanger (130) has a third hot medium channel and a third cold medium channel, wherein the inlet of the third hot medium channel is used for inputting the second-stage reaction effluent, the inlet of the third cold medium channel is connected to the outlet of the second cold medium channel, and the outlet of the third cold medium channel is used for connecting to a downstream device; The fourth heat exchanger (140) has a fourth hot medium channel and a fourth cold medium channel. The inlet of the fourth hot medium channel is connected to the outlet of the third hot medium channel. The outlet of the fourth hot medium channel is used to connect to the inlet of the hot high separation tank (500). The inlet of the fourth cold medium channel is used to supply the feed input of the second-stage reaction flow. The outlet of the fourth cold medium channel is used to supply the feed output of the second-stage reaction flow after heat exchange.

2. The heat exchange assembly according to claim 1, characterized in that: The inlet of the first cold medium channel of the first heat exchanger (110) is connected to a first feed pipeline (111) for conveying a section of reaction flow feed, and the first feed pipeline (111) is provided with a first feed valve (112) for controlling flow rate, and the outlet of the first cold medium channel is connected to a first discharge pipeline (113) for conveying a section of reaction flow feed after heat exchange; The invention also includes a first bypass pipeline (114) and a first bypass valve (115) arranged on the first bypass pipeline (114) for controlling flow rate, wherein the inlet end of the first bypass pipeline (114) is connected to the first feed pipeline (111), and the outlet end of the first bypass pipeline (114) is connected to the first discharge pipeline (113).

3. The heat exchange assembly according to claim 2, characterized in that: The first feed pipeline (111) includes a raw oil pipeline (1111) for conveying raw oil and a hydrogen pipeline (1112) for conveying hydrogen, and the outlet of the raw oil pipeline (1111) and the outlet of the hydrogen pipeline (1112) are both connected to the inlet of the first cold medium channel of the first heat exchanger (110); The inlet end of the first bypass pipeline (114) is connected to the crude oil pipeline (1111), and the first feed valve (112) is arranged on the crude oil pipeline (1111).

4. The heat exchange assembly according to claim 2, characterized in that: The inlet of the second cold medium channel of the second heat exchanger (120) is connected to a second feed pipeline (121) for conveying the stripping tower bottom liquid, and the second feed pipeline (121) is provided with a second feed valve (122) for controlling the flow rate, and the outlet of the second cold medium channel is connected to the inlet of the third cold medium channel of the third heat exchanger (130) via a second discharge pipeline (123); The invention also includes a second bypass pipeline (124) and a second bypass valve (125) arranged on the second bypass pipeline (124) for controlling flow rate. The inlet end of the second bypass pipeline (124) is connected to the second feed pipeline (121), and the outlet end of the second bypass pipeline (124) is connected to the second discharge pipeline (123).

5. The heat exchange assembly according to claim 4, characterized in that: The outlet of the third cold medium channel of the third heat exchanger (130) is connected to a third discharge pipeline (133); It also includes a third bypass pipeline (134) and a third bypass valve (135) for controlling flow rate, which is arranged on the third bypass pipeline (134); the inlet end of the third bypass pipeline (134) is connected to the second discharge pipeline (123); the outlet end of the second bypass pipeline (124) is connected to the third discharge pipeline (133); and a third feed valve (132) for controlling flow rate is arranged on the second discharge pipeline (123) between the inlet end of the third bypass pipeline (134) and the inlet of the third cold medium channel.

6. The heat exchange assembly according to claim 2, characterized in that: The inlet of the second cold medium channel of the second heat exchanger (120) is connected to a second feed pipeline (121) for conveying the stripping tower bottom liquid, and the second feed pipeline (121) is provided with a second feed valve (122) for controlling the flow rate; the outlet of the third cold medium channel of the third heat exchanger (130) is connected to a third discharge pipeline (133); It also includes a large bypass pipeline (144) and a large bypass valve (145) arranged on the large bypass pipeline (144) for controlling flow, wherein the inlet end of the large bypass pipeline (144) is connected to the second feed pipeline (121), and the outlet end of the large bypass pipeline (144) is connected to the third discharge pipeline (133).

7. The heat exchange assembly according to claim 5, characterized in that: At least one of the first bypass pipeline (114), the second bypass pipeline (124), and the third bypass pipeline (134) is arranged in the corresponding heat exchanger to form a bypass channel (2), and the outlet of the bypass channel (2) is connected to the outlet of the cold medium channel in the corresponding heat exchanger.

8. The heat exchange assembly according to claim 7, characterized in that: The heat exchanger is a wound tube heat exchanger, comprising a shell (1) and the above-mentioned cold medium channel as a shell side (101) or a tube side (102); the shell (1) is provided with a cold medium inlet pipe (100a) connected to the inlet end of the cold medium channel, a cold medium outlet pipe (100b) connected to the outlet end of the cold medium channel, and a bypass medium inlet pipe (2a) connected to the inlet end of the bypass channel (2); the outlet end of the bypass channel (2) is connected to the outlet end of the cold medium channel, and the cold medium outlet pipe (100b) is used for outputting a mixed medium obtained by mixing the cold medium and the bypass medium.

9. The heat exchange assembly according to claim 8, characterized in that: The extension direction of the bypass channel (2) is consistent with the extension direction of the cold medium channel, and the inlet end of the bypass channel (2) is relatively close to the inlet end of the cold medium channel.

10. The heat exchange assembly according to claim 9, characterized in that: The bypass channel (2) is located in the cold medium channel.

11. The heat exchange assembly according to claim 10, characterized in that: The bypass channel (2) extends up and down and is arranged as a central tube in the center of the shell (1); the heat exchange tube (3) in the tube pass (102) is spirally wound around the outer circumference of the bypass channel (2).

12. The heat exchange assembly according to claim 11, characterized in that: A switch element capable of cutting off or opening the passage in the bypass channel (2) is provided in the bypass channel (2) near its outlet end.

13. The heat exchange assembly according to claim 12, characterized in that: The switch element comprises a valve plate (23) and an elastic member (24); the valve plate (23) is rotatably arranged in the bypass channel (2) to cut off or open the passage in the bypass channel (2); the elastic member (24) acts on the valve plate (23) so that the valve plate (23) always has a tendency to rotate to cut off the passage; at the same time, under the action of the bypass medium flowing from the inlet end to the outlet end in the bypass channel (2), the valve plate (23) is arranged to overcome the elastic force of the elastic member (24) and rotate to a state of opening the passage.

14. The heat exchange assembly according to claim 13, characterized in that: A door plate (25) with a through hole (250) is horizontally placed in the bypass channel (2), and the valve plate (23) is rotatably arranged on the door plate (25). Along the flow direction of the bypass medium from the inlet end to the outlet end of the bypass channel (2), the valve plate (23) is located downstream of the door plate (25) to open and close the through hole (250). When the valve plate (23) opens the through hole (250), the passage in the bypass channel (2) is connected, and when the valve plate (23) closes the through hole (250), the passage in the bypass channel (2) is cut off.

15. The heat exchange assembly according to claim 14, characterized in that: The edge of one side of the valve plate (23) is rotatably connected to the door plate (25) via a rotating shaft (231), and the elastic member (24) is a torsion spring sleeved on the outer periphery of the rotating shaft (231).

16. The heat exchange assembly according to claim 11, characterized in that: The shell (1) is provided with two tube sheets (5) for supporting the upper and lower ends of the heat exchange tubes (3); at least one end of the bypass channel (2) is constrained on the tube sheet (5) in a manner that it can be telescopically moved up and down relative to the corresponding tube sheet (5).

17. A hydrogenation system, comprising a fractionation tower (200), a stripping tower (300), a heating furnace (400), a hot high separation tank (500) and a first heat exchange device (600), characterized in that It also has a heat exchange component as claimed in any one of claims 1 to 16, wherein the inlet of the second cold medium channel of the second heat exchanger (120) is connected to the outlet at the bottom of the stripping tower (300), the inlet of the hot high separation tank (500) is connected to the outlet of the second hot medium channel of the second heat exchanger (120) and the outlet of the fourth hot medium channel of the fourth heat exchanger (140), the outlet at the top of the hot high separation tank (500) is connected to the inlet of the hot medium channel of the first heat exchange device (600), the inlet of the cold medium heat exchange channel of the first heat exchange device (600) is connected to a stripping tower feed pipeline (310) for conveying stripping tower feed, and the outlet of the cold medium heat exchange channel of the first heat exchange device (600) is connected to the feed port of the stripping tower (300); The outlet of the third cold medium channel of the third heat exchanger (130) is connected to the input end of the heating furnace (400), and the output end of the heating furnace (400) is connected to the feed inlet of the distillation tower (200).

18. The hydrogenation system according to claim 17, characterized in that: It also includes a second heat exchange device (700), the inlet of its cold medium heat exchange channel is connected to the outlet of the third cold medium channel of the third heat exchanger (130), the outlet of its cold medium heat exchange channel is connected to the input end of the heating furnace (400), and the inlet of its hot medium heat exchange channel is connected to the outlet at the bottom of the distillation tower (200).

19. The hydrogenation system according to claim 18, characterized in that: It also includes a third heat exchange device (800), the inlet of its hot medium heat exchange channel is connected to the outlet of the hot medium heat exchange channel of the second heat exchange device (700), and the inlet of its cold medium heat exchange channel is connected to a water supply pipeline (810) for conveying water.

20. The hydrogenation system according to claim 17, characterized in that: The first heat exchange device (600) has three cold medium heat exchange channels, wherein the inlet of the first cold medium heat exchange channel is connected to a hydrogen supply pipeline (610) for transporting hydrogen, the inlet of the second cold medium heat exchange channel is connected to the above-mentioned stripping tower feed pipeline (310), and the inlet of the third cold medium heat exchange channel is connected to a water supply pipeline (620) for transporting water. The first cold medium heat exchange channel, the second cold medium heat exchange channel, and the third cold medium heat exchange channel are arranged in sequence along the flow direction of the hot high-fraction gas in the hot medium channel of the first heat exchange device (600).

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