A heat exchange assembly and hydrogenation system for hydrorefining of diesel and wax oil

Abstract

The application discloses a heat exchange assembly and a hydrogenation system for diesel and wax oil hydrogenation, and the heat exchange assembly comprises a first heat exchanger, an inlet of a first heat medium channel of the first heat exchanger is used for inputting a first reaction effluent, an inlet of a first cold medium channel of the first heat exchanger is used for inputting a first reaction feed, and an outlet of the first cold medium channel is used for outputting the first reaction feed after heat exchange; a second heat exchanger, an inlet of a second heat medium channel of the second heat exchanger is communicated with an outlet of the first heat medium channel, an outlet of the second heat medium channel is used for being communicated with an inlet of a hot high separation tank, and an inlet of a second cold medium channel of the second heat exchanger is used for inputting a stripping tower bottom liquid; a third heat exchanger, an inlet of a third heat medium channel of the third heat exchanger is used for inputting a second reaction effluent, an inlet of a third cold medium channel of the third heat exchanger is communicated with an outlet of the second cold medium channel, and an outlet of the third cold medium channel is used for being communicated with downstream equipment; and a fourth heat exchanger. Compared with the prior art, the application can reduce equipment investment and improve heat exchange efficiency.

Description

Technical Field

[0001] This invention belongs to the field of petroleum processing technology, specifically relating to a heat exchange component and hydrogenation system for diesel oil hydrogenation. Background Technology

[0002] Existing systems for hydrogenating diesel oil, such as Figure 1 As shown, it uses a traditional shell and tube heat exchanger, which has a series of problems such as low heat exchange efficiency, easy internal leakage, and difficulty in large-scale equipment. It requires a large heat exchange temperature difference to cut the hot and cold streams at multiple temperature positions to achieve heat transfer design and equipment manufacturability. This results in a large number of heat exchange equipment, high-pressure pipelines, high-pressure sealing surfaces, large footprint, difficult piping work, and large total investment in equipment frame design and equipment cost. Summary of the Invention

[0003] The first technical problem to be solved by the present invention is to provide a heat exchange component for diesel oil hydrogenation, in order to reduce equipment investment and improve heat exchange efficiency, in light of the current state of the prior art.

[0004] The second technical problem to be solved by the present invention is to provide a hydrogenation system having the above-mentioned heat exchange components.

[0005] The technical solution adopted by the present invention to solve the first technical problem mentioned above is: a heat exchange component for diesel oil hydrogenation, characterized in that it comprises:

[0006] The first heat exchanger has a first hot medium channel and a first cold medium channel. The inlet of the first hot medium channel is used to input a section of reaction effluent, the inlet of the first cold medium channel is used to input a section of reaction feed, and the outlet of the first cold medium channel is used to output a section of reaction feed after heat exchange.

[0007] 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-temperature separator. The inlet of the second cold medium channel is used to supply the bottom liquid of the stripping tower.

[0008] The third heat exchanger has a third hot medium channel and a third cold medium channel. The inlet of the third hot medium channel is used to input the effluent from the second stage reaction. The inlet of the third cold medium channel is connected to the outlet of the second cold medium channel. The outlet of the third cold medium channel is used to connect to downstream equipment.

[0009] 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 hot medium channel. The outlet of the fourth hot medium channel is used to connect to the inlet of the high-temperature separation tank. The inlet of the fourth cold medium channel is used to supply the second-stage reaction flow feed. The outlet of the fourth cold medium channel is used to supply the second-stage reaction flow feed after heat exchange.

[0010] The design and connection of the four heat exchangers in this invention effectively increases the outlet temperature of the first-stage and second-stage reaction feeds, thereby reducing the load on the subsequent high-pressure reaction furnace, which reduces the investment in the high-pressure furnace. Furthermore, this invention prioritizes heat exchange between the low-temperature, low-pressure stripper bottom liquid and the high-pressure reaction effluent, expanding the heat transfer temperature difference of the high-pressure heat exchangers and reducing equipment investment in the high-pressure section. Simultaneously, the second-stage reaction effluent first exchanges heat with the stripper bottom liquid, which helps to increase the temperature of the stripper bottom liquid. In summary, this invention reduces the number of heat exchangers while improving heat exchange efficiency, resulting in a smaller system footprint, easier piping, and a significant reduction in total investment.

[0011] 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 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 a section of reaction flow feed after heat exchange.

[0012] It also includes a first bypass pipeline and a first bypass valve disposed on the first bypass pipeline for controlling the flow rate. The inlet end of the first bypass pipeline is connected to the first feed pipeline, and the outlet end of the first bypass pipeline is connected to the first discharge pipeline.

[0013] Preferably, the first feed line includes a raw oil pipeline for conveying raw oil and a hydrogen pipeline for conveying 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.

[0014] The inlet end of the first bypass pipeline is connected to the raw material oil pipeline, and the first feed valve is located on the raw material oil pipeline.

[0015] Preferably, the inlet of the second cold medium channel of the second heat exchanger is connected to a second feed pipeline for conveying the bottom liquid of the stripping tower, and a second feed valve for controlling the flow rate is provided on the second feed pipeline. The outlet of the second cold medium channel is connected to the inlet of the third cold medium channel of the third heat exchanger through a second discharge pipeline.

[0016] It also includes a second bypass pipeline and a second bypass valve installed on the second bypass pipeline for controlling the flow rate. The inlet end of the second bypass pipeline is connected to the second feed pipeline, and the outlet end of the second bypass pipeline is connected to the second discharge pipeline.

[0017] Preferably, the outlet of the third cold medium channel of the third heat exchanger is connected to a third discharge pipeline;

[0018] It also includes a third bypass pipeline and a third bypass valve for controlling the flow rate, wherein 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 the 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.

[0019] In the above scheme, preferably, the inlet of the second cold medium channel of the second heat exchanger is connected to a second feed pipeline for conveying the bottom liquid of the stripping tower, 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.

[0020] It also includes a large bypass pipeline and a large bypass valve installed on the large bypass pipeline for controlling the flow rate. 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.

[0021] In the aforementioned heat exchange components, the stripping tower bottom liquid or feed oil serves as the cold fluid flowing through the heat exchanger's cold medium channel and bypass pipelines. However, the design of bypass pipelines and bypass valves must consider factors such as the site framework and pipe racks. Bypass pipelines are often long, with significant bypass level differences, resulting in a pressure drop in the bypass that exceeds the pressure drop of the fluid flowing through the heat exchange equipment. This makes it impossible to properly regulate the bypass pipelines, causing the temperature of the cold fluid after heat exchange to exceed the design requirements, impacting the subsequent heat exchange network and operation. Furthermore, if the temperature of the cold fluid after heat exchange is too high, exceeding the maximum temperature the pipeline can withstand, it can lead to leaks or even explosions, posing a safety hazard.

[0022] Therefore, in the above solutions, to improve safety, preferably, at least one of the first bypass pipeline, the second bypass pipeline, and the third bypass pipeline is located within the corresponding heat exchanger to form a bypass channel, and the outlet of the bypass channel is connected to the outlet of the cold medium channel within the corresponding heat exchanger. In this way, the bypass medium can be mixed with the cooled fluid after heat exchange before being output, and the temperature of the mixed medium is lower than that of the cooled fluid after heat exchange, thereby solving the safety problem caused by excessively high temperature of the cooled fluid after heat exchange.

[0023] Preferably, the heat exchanger is a wound tube heat exchanger, including a shell and the aforementioned cold medium passage as the shell side or tube side. The shell is provided with a cold medium inlet pipe connected to the inlet end of the cold medium passage, a cold medium outlet pipe connected to the outlet end of the cold medium passage, and a bypass medium inlet pipe connected to the inlet end of the bypass passage. The outlet end of the bypass passage is connected to the outlet end of the cold medium passage, and the cold medium outlet pipe supplies the mixed medium after the cold medium and the bypass medium are mixed.

[0024] Furthermore, the extension direction of the bypass channel is consistent with the extension direction of the cold medium channel, and the inlet end of the bypass channel is relatively close to the inlet end of the cold medium channel.

[0025] Furthermore, the bypass channel is located within the cold medium channel.

[0026] To improve structural compactness, preferably, the bypass channel extends vertically and is located in the center of the shell as a central cylinder; the heat exchange tubes in the tube side are spirally wound around the outer periphery of the bypass channel.

[0027] In the above scheme, in order to avoid backflow of the medium in the bypass channel without affecting the normal delivery of the bypass medium, preferably, a switch that can cut off or open the passage in the bypass channel is provided near its outlet end in the bypass channel.

[0028] Preferably, the switching element includes a valve plate and an elastic element. The valve plate is rotatably disposed in the bypass channel to cut off or open the passage in the bypass channel. The elastic element acts on the valve plate so that the valve plate always has the 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 element and rotate to the state of opening the passage.

[0029] In this way, the valve plate can prevent the bypass medium from flowing back into the bypass, and when the bypass medium is flowing normally in the bypass, the bypass medium can push open the valve plate and open the passage, thus not affecting the normal transportation of the bypass medium.

[0030] Preferably, a door plate with a through hole is horizontally placed in the bypass channel, and the valve plate is rotatably disposed on the door plate. Along the flow direction of the bypass medium from the inlet end to the outlet end of the bypass channel, the valve plate is located downstream of the door plate to open and close the through hole. When the valve plate opens the through hole, the passage in the bypass channel is open, and when the valve plate closes the through hole, the passage in the bypass channel is cut off.

[0031] Furthermore, one edge of the valve plate is rotatably connected to the door panel via a pivot, and the elastic element is a torsion spring sleeved on the outer periphery of the pivot.

[0032] Furthermore, the housing 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 allows it to extend and retract relative to the corresponding tube sheet.

[0033] The technical solution adopted by the present invention to solve the second technical problem mentioned above is as follows: a hydrogenation system, comprising a fractionation tower, a stripping tower, a heating furnace, a hot-high-temperature separation tank, and a first heat exchange device, characterized in that it further comprises the heat exchange components as described above, wherein 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-temperature 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-temperature 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 the feed of the stripping tower, and the outlet of the cold medium heat exchange channel of the first heat exchange device is connected to the feed inlet of the stripping tower;

[0034] 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 fractionation tower.

[0035] Preferably, the system further includes a second heat exchange device, the inlet of which is connected to the outlet of the third cold medium channel of the third heat exchanger, the outlet of which is connected to the input end of the heater, and the inlet of which is connected to the outlet of the bottom of the fractionation tower. In this way, the unconverted oil at the bottom of the fractionation tower can be used to heat the bottom liquid of the stripping tower, reducing the load on the heater before the feed to the fractionation tower.

[0036] Furthermore, it also includes a third heat exchange device, the inlet of which is connected to the outlet of the heat exchange channel of the second heat exchange device, and the inlet of which is connected to a water supply pipeline for conveying water.

[0037] 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 feed pipeline of the stripping tower mentioned above, 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-temperature gas in the hot medium channel of the first heat exchange device. In this way, the heat of the hot high-temperature gas can be fully utilized.

[0038] Compared with existing technologies, the advantages of this invention are as follows: The design and connection of the four heat exchangers in this invention can effectively increase the outlet temperature of the first-stage and second-stage reaction stream feeds, thereby reducing the load on the subsequent high-pressure reaction furnace, i.e., reducing the investment in the high-pressure furnace; Furthermore, this invention prioritizes heat exchange between the low-temperature, low-pressure stripper bottom liquid and the high-pressure reaction effluent, expanding the heat transfer temperature difference of the high-pressure heat exchangers and reducing the equipment investment in the high-pressure heat exchangers; At the same time, the second-stage reaction effluent first exchanges heat with the stripper bottom liquid, which helps to increase the temperature of the stripper bottom liquid; In summary, this invention reduces the number of heat exchangers while improving heat exchange efficiency, resulting in a smaller system footprint, convenient piping, and a significant reduction in total investment. Attached Figure Description

[0039] Figure 1 This is a schematic diagram of the structure of a hydrogenation system in the prior art;

[0040] Figure 2 This is a schematic diagram of the hydrogenation system in Embodiment 1 of the present invention;

[0041] Figure 3 This is a schematic diagram of the heat exchange component in Embodiment 2 of the present invention (corresponding to...). Figure 2 (The part within the dashed box);

[0042] Figure 4 This is a schematic diagram of the heat exchange component in Embodiment 3 of the present invention (corresponding to...). Figure 2 (The part within the dashed box);

[0043] Figure 5 This is a schematic diagram of the heat exchange component in Embodiment 4 of the present invention (corresponding to...). Figure 2 (The part within the dashed box);

[0044] Figure 6 This is a schematic diagram of the heat exchanger in Embodiment 4 of the present invention;

[0045] Figure 7 This is a schematic diagram of the heat exchanger in Embodiment 5 of the present invention;

[0046] Figure 8 This is a schematic diagram of the heat exchanger in Embodiment Six of the present invention;

[0047] Figure 9 for Figure 8 Enlarged view of section A;

[0048] Figure 10 for Figure 8 Sectional view of section A. Detailed Implementation

[0049] The present invention will be further described in detail below with reference to the accompanying drawings and embodiments.

[0050] Example 1:

[0051] like Figure 2 As shown, this is a preferred embodiment of a heat exchange component and hydrogenation system for diesel fuel oil hydrogenation according to the present invention. The hydrogenation system includes a heat exchange component, a fractionation tower 200, a stripping tower 300, a heating furnace 400, a hot-high heat separation tank 500, and a first heat exchange device 600, a second heat exchange device 700, and a third heat exchange device 800.

[0052] The heat exchange components include a first heat exchanger 110, a second heat exchanger 120, a third heat exchanger 130, and a fourth heat exchanger 140.

[0053] 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 input a section of reaction effluent, the inlet of the first cold medium channel is used to input a section of reaction feed, the outlet of the first cold medium channel is used to output a section of reaction feed after heat exchange, and the outlet of the first cold medium channel is used to connect to a reverse feed heating furnace.

[0054] 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 temperature separator 500. The inlet of the second cold medium channel is connected to the outlet at the bottom of the stripping tower 300.

[0055] 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 to input the effluent from the second stage reaction, 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.

[0056] 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 high-temperature separation tank 500. The inlet of the fourth cold medium channel is used for the input of the second-stage reaction flow feed. The outlet of the fourth cold medium channel is used for the output of the second-stage reaction flow feed after heat exchange. The outlet of the fourth cold medium channel is connected to the second-stage reaction feed heater.

[0057] The aforementioned 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-temperature separator 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 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 a stripper feed pipeline 310 for transporting stripper 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-temperature gas in the hot medium channel of the first heat exchange device 600.

[0058] The aforementioned stripping tower 300 is a desulfurized hydrogen stripping tower, and its inlet is connected to the outlet of the second cold medium heat exchange channel of the first heat exchange device 600. The stripping tower 300 also has a steam inlet at its lower part.

[0059] The outlet of the third cold medium channel of the third heat exchanger 130 is connected to the feed inlet of the fractionation tower 200 via the second heat exchange device 700, the heating furnace 400, and the fractionation tower 200. 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 inlet of the fractionation 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 fractionation tower 200.

[0060] The inlet of the heat medium heat exchange channel of the third heat exchange device 800 is connected to the outlet of the heat 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.

[0061] The heat exchange process in this embodiment is as follows:

[0062] A reaction effluent flows sequentially through the first heat medium channel of the first heat exchanger 110 and the second heat medium channel of the second heat exchanger 120 before entering the high-temperature separation tank 500. The temperature of the 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 reaction effluent exiting from the second heat medium channel of the second heat exchanger 120 is 255°C. Simultaneously, a reaction feed (temperature 207°C, pressure 19.54 MPa) is fed into the first cold medium channel of the first heat exchanger 110 to exchange heat with the reaction effluent. The heat-exchanged reaction feed (temperature 405°C) is then sent to the first reverse feed heater.

[0063] The effluent from the second-stage reaction sequentially 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 before entering the high-temperature 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 exiting from the fourth heat medium channel of the fourth heat exchanger 140 is 255°C. Simultaneously, the feed stream of the second-stage reaction (temperature 216°C, pressure 18.3 MPa) enters the fourth cold medium channel of the fourth heat exchanger 140 to exchange heat with the second-stage reaction effluent. The feed stream of the second-stage reaction after heat exchange (temperature 380°C) is then sent to the second-stage reaction feed heater.

[0064] The hot high-temperature gas (pressure 16.4 MPa) output from the top of the hot high-temperature separator 500 passes through the hot medium channel of the first heat exchanger 600 and is then output to the air cooler. The temperature of the hot high-temperature gas output from the hot medium channel of the first heat exchanger 600 is 90°C. Simultaneously, hydrogen enters the first cold medium heat exchange channel of the first heat exchanger 600 through the hydrogen supply pipeline 610 to exchange heat with the hot high-temperature gas. The temperature of the hydrogen before heat exchange is 87°C, and the temperature after heat exchange is 20°C. 0.7℃; 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-temperature gas. The temperature of the stripping tower feed before heat exchange is 49℃, and the temperature of the stripping tower feed after heat exchange is 166.6℃; 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-temperature gas. The water temperature before heat exchange is 70℃, and the water temperature after heat exchange is 95℃.

[0065] The stripping column bottom liquid output from the bottom of the stripping column passes sequentially 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 heater 400 before entering the fractionation column 200. The temperature of the stripping column bottom liquid output from the bottom of the stripping column is 213℃ and the pressure is 3.0MPa. The temperature of the stripping column bottom liquid output from the second cold medium channel of the second heat exchanger 120 is 276℃. The temperature of the stripping column bottom liquid output from the third cold medium channel of the third heat exchanger 130 is 282.4℃. The temperature of the stripping column bottom liquid output from the cold medium heat exchange channel of the second heat exchange device 700 is 307.5℃.

[0066] Simultaneously, the unconverted oil output from the bottom of the fractionation tower passes sequentially through the heat exchange channels of the second heat exchanger 700 and the third heat exchanger 800 before being output. The temperature of the unconverted oil output from the bottom of the fractionation tower is 354℃, and the pressure is 1.6MPa. The temperature of the unconverted oil output from the heat exchange channel of the second heat exchanger 700 is 287.5℃, and the temperature of the unconverted oil output from the heat exchange channel of the third heat exchanger 800 is 240℃. At the same time, 70℃ water enters the cold medium channel of the third heat exchanger 800 through the water supply pipeline 810, exchanges heat with the unconverted oil, and is then output at a temperature of 95℃.

[0067] 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 on the subsequent high-pressure reaction heating furnace, which means that the investment in the high-pressure section heating furnace is reduced.

[0068] Furthermore, a temperature rise of 10-15°C is reserved for the reaction feed heater, which is beneficial for adjusting for changes in operating conditions. In addition, the large bypass for the feed oil and stripping tower bottom liquid makes the entire system adjustment more convenient and effective.

[0069] Compared to existing technologies, the design load of the low-pressure heating furnace 400 in this embodiment needs to be increased, but because the pressure is low, the increase in cost is not significant.

[0070] Furthermore, in this embodiment, by exchanging heat between the hot high-temperature gas and the stripping tower feed, the stripping tower feed temperature can be increased, thereby effectively reducing the amount of steam used in the stripping tower.

[0071] By designing the second heat exchange device 700, the temperature difference between the unconverted oil and the bottom liquid of the stripping tower is reduced, which can reduce the load on the heating furnace 400 before the feed to the fractionation tower.

[0072] Example 2:

[0073] like Figure 3 The image shows a preferred embodiment of the heat exchange component and hydrogenation system for diesel fuel oil hydrogenation according to the present invention. This embodiment is basically the same as the first embodiment, except that the inlet of the second cold medium channel of the second heat exchanger 120 is connected to a second feed line 121 for conveying the bottom liquid of the stripping tower, and a second feed valve 122 for controlling the flow rate is provided on the second feed line 121. 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 through a second discharge line 123; the outlet of the third cold medium channel of the third heat exchanger 130 is connected to a third discharge line 133.

[0074] It also includes a second bypass line 124 and a second bypass valve 125 installed on the second bypass line 124 for controlling the flow rate. The inlet end of the second bypass line 124 is connected to the second feed line 121, and the outlet end of the second bypass line 124 is connected to the second discharge line 123 near the outlet of the second cold medium channel of the second heat exchanger 120.

[0075] It also includes a third bypass line 134 and a third bypass valve 135 for controlling the flow rate, which is provided on the third bypass line 134. The inlet end of the third bypass line 134 is connected to the inlet of the third cold medium channel of the second discharge line 123 near the inlet of the third cold medium channel of the third heat exchanger 130. The outlet end of the second bypass line 124 is connected to the third discharge line 133. A third feed valve 132 for controlling the flow rate is provided on the second discharge line 123 at the position between the inlet end of the third bypass line 134 and the inlet of the third cold medium channel.

[0076] Example 3:

[0077] like Figure 4 The image shows a preferred embodiment three of the heat exchange component and hydrogenation system for diesel fuel oil hydrogenation according to the present invention. This embodiment is basically the same as embodiment one, except that 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 reaction flow feed 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 reaction flow feed. The first feed pipeline 111 includes a raw oil pipeline 1111 for conveying raw oil and a hydrogen pipeline 1112 for conveying hydrogen. The outlets of the raw oil pipeline 1111 and the hydrogen pipeline 1112 are both connected to the inlet of the first cold medium channel of the first heat exchanger 110, and a first feed valve 112 for controlling the flow rate is provided on the raw oil pipeline 1111.

[0078] It also includes a first bypass pipeline 114 and a first bypass valve 115 installed on the first bypass pipeline 114 for controlling the flow rate. The inlet end of the first bypass pipeline 114 is connected to the raw material oil pipeline 1111, and the outlet end of the first bypass pipeline 114 is connected to the first discharge pipeline 113.

[0079] Meanwhile, the inlet of the second cold medium channel of the second heat exchanger 120 is connected to a second feed line 121 for conveying the bottom liquid of the stripping tower, and a second feed valve 122 for controlling the flow rate is provided on the second feed line 121; the outlet of the third cold medium channel of the third heat exchanger 130 is connected to a third discharge line 133.

[0080] It also includes a large bypass pipeline 144 and a large bypass valve 145 installed 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.

[0081] Example 4:

[0082] like Figure 5 , 6 The image shows a preferred embodiment four of the heat exchange component and hydrogenation system for diesel fuel oil hydrogenation according to the present invention. This embodiment is basically the same as embodiment two, except that 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 reaction flow feed 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 reaction flow feed. The first feed pipeline 111 includes a raw oil pipeline 1111 for conveying raw oil and a hydrogen pipeline 1112 for conveying hydrogen. The outlets of the raw oil pipeline 1111 and the hydrogen pipeline 1112 are both connected to the inlet of the first cold medium channel of the first heat exchanger 110, and a first feed valve 112 for controlling the flow rate is provided on the raw oil pipeline 1111.

[0083] It also includes a first bypass pipeline 114 and a first bypass valve 115 installed on the first bypass pipeline 114 for controlling the flow rate. The inlet end of the first bypass pipeline 114 is connected to the raw material oil pipeline 1111, and the outlet end of the first bypass pipeline 114 is connected to the first discharge pipeline 113.

[0084] In this embodiment, the first bypass pipeline 114, the second bypass pipeline 124, and the third bypass pipeline 134 are respectively located in their respective heat exchangers to form three bypass channels 2. The outlet of each bypass channel 2 is connected to the outlet of the cold medium channel in the corresponding heat exchanger. Specifically:

[0085] Each heat exchanger is a wound tube heat exchanger and includes a shell 1, a bypass channel 2 and heat exchange tubes 3.

[0086] The shell 1 is a vertically arranged cylindrical shape, with a cold medium inlet pipe 100a and a cold medium outlet pipe 100b respectively located at its upper and lower ends. Simultaneously, a shell-side inlet pipe 1a for heating medium input is located at the lower part of the side wall of the shell 1, and a shell-side outlet pipe 1b for heating medium output is located at the upper part of the side wall of the shell 1. The shell-side inlet pipe 1a and shell-side outlet pipe 1b are connected to the interior of the shell 1 (which serves as the shell side 101 of the heat exchanger).

[0087] The bypass channel 2 extends vertically and serves as the central cylinder within the housing 1. Tube sheets 5 are respectively installed at both ends of the bypass channel 2 within the housing 1. The lower end of the bypass channel 2 is located above the corresponding tube sheet 2 and the two are fixed together. The lower port 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 inserted together, allowing the upper end of the bypass channel 2 to move vertically and horizontally relative to the tube sheet 5. At the same time, the upper end of the bypass channel 2 is connected to the cold medium inlet pipe 100a.

[0088] The heat exchange tube 3, as the tube side 102 (i.e., cold medium channel) of the heat exchanger, is wound around the outer periphery of the bypass channel 2. The upper and lower ends of the heat exchange tube 3 are respectively supported on the corresponding tube sheet 2 and are respectively connected to the corresponding cold medium inlet pipe 100a and cold medium outlet pipe 100b.

[0089] Meanwhile, a bypass medium inlet pipe 2a is provided on the upper part of the shell 1, relatively close to the cold medium inlet pipe 100a. A portion of the bypass medium inlet pipe 2a passes downward through the corresponding tube sheet 5 and extends 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, and the cold medium outlet pipe 100b supplies the mixed medium after the cold medium and the bypass medium are mixed.

[0090] During operation, the hot medium enters the shell 1 through the shell-side inlet pipe 1a, exchanges heat with the cold medium, and then exits through the shell-side outlet pipe 1b. The bypass medium enters the bypass channel 2 through the bypass medium inlet pipe 2a, and the cold medium enters the heat exchange tube 3 through the cold medium inlet pipe 100a. After exchanging heat with the hot medium, the cold medium flows out of the heat exchange tube 3 and mixes with the bypass medium before exiting together through the cold medium outlet pipe 100b.

[0091] Example 5:

[0092] like Figure 7 The image shows a preferred embodiment five of the heat exchange component and hydrogenation system for diesel oil hydrogenation according to the present invention. This embodiment is basically the same as embodiment four, except that in this embodiment:

[0093] The shell 1 is a vertically arranged cylindrical shape, with a cold medium outlet pipe 100b and a cold medium inlet pipe 100a respectively at the upper and lower ends. At the same time, the upper part of the side wall of the shell 1 is provided with a shell-side inlet pipe 1a for the input of the heating medium, and the lower part of the side wall of the shell 1 is provided with a shell-side outlet pipe 1b for the output of the heating medium. The shell-side inlet pipe 1a and the shell-side outlet pipe 1b are connected to the interior of the shell 1 (which serves as the shell side 101 of the heat exchanger).

[0094] The bypass channel 2 extends vertically and is located in the center of the housing 1 as a central cylinder; and tube sheets 5 are respectively provided at both ends of the bypass channel 2 within the housing 1. The lower end of the bypass channel 2 is located above the corresponding tube sheet 2 and the two are fixed together; the upper end of the bypass channel 2 is located below the corresponding tube sheet 5 and the two are inserted together, so that the upper end of the bypass channel 2 can move and extend vertically relative to the tube sheet 5. At the same time, the upper port of the bypass channel 2 is connected to the cold medium outlet pipe 100b.

[0095] The heat exchange tube 3, as the tube side 102 (i.e., cold medium channel) of the heat exchanger, is wound around the outer periphery of the bypass channel 2. The upper and lower ends of the heat exchange tube 3 are respectively supported on the corresponding tube sheet 2 and are respectively connected to the corresponding cold medium outlet pipe 100b and cold medium inlet pipe 100a.

[0096] Meanwhile, a bypass medium inlet pipe 2a is provided at the lower part of the shell 1, relatively close to the cold medium inlet pipe 100a. A portion of the bypass medium inlet pipe 2a passes upward through the corresponding tube sheet 5 and extends 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, and the cold medium outlet pipe 100b supplies the mixed medium after the tube-side medium and the bypass medium are mixed.

[0097] During operation, the hot medium enters the shell 1 through the shell-side inlet pipe 1a, exchanges heat with the cold medium, and then exits through the shell-side outlet pipe 1b. The bypass medium enters the bypass channel 2 through the bypass medium inlet pipe 2a, and the cold medium enters the heat exchange tube 3 through the cold medium inlet pipe 100a. After exchanging heat with the hot medium, the cold medium flows out of the heat exchange tube 3 and mixes with the bypass medium before exiting together through the cold medium outlet pipe 100b.

[0098] Example 6:

[0099] like Figures 8-10 The image shows a preferred embodiment six of the present invention for a heat exchange component and hydrogenation system for diesel oil hydrogenation. This embodiment is basically the same as embodiment four, except that in this embodiment:

[0100] The spiral wound tube heat exchanger includes a shell 1, a bypass channel 2, a switching element and heat exchange tubes 3.

[0101] The shell 1 is a vertically arranged cylindrical shape. The upper and lower ends of the shell 1 are respectively provided with a tube-side inlet pipe for inputting the tube-side medium and a tube-side outlet pipe for outputting the tube-side medium. Simultaneously, the lower part of the side wall of the shell 1 is provided with a cold medium inlet pipe 100a for inputting the cold medium, and the upper part of the side wall of the shell 1 is provided with a cold medium outlet pipe 100b for outputting the cold medium. The cold medium inlet pipe 100a and the cold medium outlet pipe 100b are connected to the interior of the shell 1 (which serves as the shell side 101 of the heat exchanger, i.e., the cold medium channel).

[0102] The bypass channel 2 extends vertically and is located in the center of the housing 1 as a central cylinder; and tube sheets 5 are respectively provided at both ends of the bypass channel 2 inside the housing 1. The lower end of the bypass channel 2 (as the inlet end of the bypass channel 2) is located above the corresponding tube sheet 2 and the two are fixed together; the upper end of the bypass channel 2 (as the outlet end of the bypass channel 2) is located below the corresponding tube sheet 5 and the two are inserted together so that the upper end of the bypass channel 2 can move vertically and horizontally relative to the tube sheet 5.

[0103] The heat exchange tube 3, as the tube side 102 of the heat exchanger, is wound around the outer periphery of the bypass channel 2. The upper and lower ends of the heat exchange tube 3 are respectively supported on the corresponding tube sheet 2 and are respectively connected to the corresponding tube side inlet pipe and tube side outlet pipe.

[0104] Meanwhile, a bypass medium inlet pipe 2a is provided on the lower part 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 (as the outlet end of the bypass channel 2). The fluid outlet 22 is opposite to the cold medium outlet pipe 100b, and the two are connected through the internal space of the housing 1. That is, the cold medium outlet pipe 100b supplies the mixed medium after the cold medium and the bypass medium are mixed.

[0105] During operation, the hot medium enters the heat exchange tube 3 through the tube inlet pipe, exchanges heat with the cold medium, and then flows out of the heat exchange tube 3. The bypass medium enters the bypass channel 2 through the bypass medium inlet pipe 2a. The cold medium enters the shell 1 through the cold medium inlet pipe 100a, exchanges heat with the hot medium, mixes with the bypass medium, and is then output through the cold medium outlet pipe 100b.

[0106] The aforementioned switch is located within the bypass channel 2, near its upper end and below the fluid outlet 22. Specifically, a door plate 25 with a through hole 250 is horizontally positioned within the bypass channel 2 corresponding to the position of the switch. The switch includes a valve plate 23 and an elastic element 24. One edge of the valve plate 23 is rotatably connected to the door plate 25 via a pivot 231 to open and close the through hole 250. When the valve plate 23 opens the through hole 250, the passage within the bypass channel 2 is open; when the valve plate 23 closes the through hole 250, the passage within the bypass channel 2 is closed. The elastic element 24 is a torsion spring sleeved around the pivot 231, ensuring that the valve plate 23 always tends to rotate to close the through hole 250. Simultaneously, under the action of the bypass medium flowing upwards within the bypass channel 2, the valve plate 23 is arranged to overcome the elastic force of the elastic element 24 and rotate to open the passage. Thus, the valve plate 23 can only open the through hole 250 under the action of the bypass medium flowing from bottom to top, thereby opening the passage in the bypass channel 2.

[0107] The specification and claims of this invention use terms indicating direction, such as "front," "rear," "upper," "lower," "left," "right," "side," "top," and "bottom," to describe various exemplary structural parts and elements of the invention. However, these terms are used herein merely for ease of explanation and are determined based on the exemplary orientations shown in the accompanying drawings. Since the embodiments disclosed in this invention can be arranged in different orientations, these terms indicating direction are for illustrative purposes only and should not be considered as limitations. For example, "upper" and "lower" are not necessarily limited to directions opposite to or consistent with the direction of gravity.

[0108] The term "vertical" is also used in the specification and claims of this invention, meaning basically along the up and down direction, and is not limited to just the vertical direction, but can also be slightly deviated from the vertical direction.

Claims

1. A heat exchange component for hydrogenation of diesel fuel oil, characterized in that... Including: 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 input a section of reaction effluent, the inlet of the first cold medium channel is used to input a section of reaction feed, and the outlet of the first cold medium channel is used to output a section of reaction feed after heat exchange. 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. The outlet of the second hot medium channel is used to connect to the inlet of the high-temperature separation tank (500). The inlet of the second cold medium channel is used to supply the bottom liquid of the stripping tower. 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 to input the effluent from the second stage reaction. The inlet of the third cold medium channel is connected to the outlet of the second cold medium channel. The outlet of the third cold medium channel is used to connect to downstream equipment. 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 high-temperature separation tank (500). The inlet of the fourth cold medium channel is used to supply the second-stage reaction flow feed. The outlet of the fourth cold medium channel is used to supply the second-stage reaction flow feed after heat exchange.

2. The heat exchange component 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 line (111) for conveying a section of reaction flow feed, and the first feed line (111) is provided with a first feed valve (112) for controlling the flow rate. The outlet of the first cold medium channel is connected to a first discharge line (113) for conveying a section of reaction flow feed after heat exchange. It also includes a first bypass line (114) and a first bypass valve (115) disposed on the first bypass line (114) for controlling the flow rate. The inlet end of the first bypass line (114) is connected to the first feed line (111), and the outlet end of the first bypass line (114) is connected to the first discharge line (113).

3. The heat exchange component according to claim 2, characterized in that: The first feed line (111) includes a raw oil line (1111) for conveying raw oil and a hydrogen line (1112) for conveying hydrogen. The outlet of the raw oil line (1111) and the outlet of the hydrogen line (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 raw material oil pipeline (1111), and the first feed valve (112) is located on the raw material 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 line (121) for conveying the bottom liquid of the stripping tower, and a second feed valve (122) for controlling the flow rate is provided on the second feed line (121). 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) through a second discharge line (123). It also includes a second bypass line (124) and a second bypass valve (125) provided on the second bypass line (124) for controlling the flow rate. The inlet end of the second bypass line (124) is connected to the second feed line (121), and the outlet end of the second bypass line (124) is connected to the second discharge line (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 the flow rate, wherein the inlet end of the third bypass pipeline (134) is connected to the second discharge pipeline (123), 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) at a position 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 line (121) for conveying the bottom liquid of the stripping tower, and a second feed valve (122) for controlling the flow rate is provided on the second feed line (121); the outlet of the third cold medium channel of the third heat exchanger (130) is connected to a third discharge line (133); It also includes a large bypass pipeline (144) and a large bypass valve (145) installed 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).

7. The heat exchange assembly according to claim 5, characterized in that: At least one of the first bypass line (114), the second bypass line (124), and the third bypass line (134) is provided 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, including a shell (1) and the aforementioned cold medium passage as the shell side (101) or tube side (102). The shell (1) is provided with a cold medium inlet pipe (100a) connected to the inlet end of the cold medium passage, a cold medium outlet pipe (100b) connected to the outlet end of the cold medium passage, and a bypass medium inlet pipe (2a) connected to the inlet end of the bypass passage (2). The outlet end of the bypass passage (2) is connected to the outlet end of the cold medium passage, and the cold medium outlet pipe (100b) supplies the mixed medium after the cold medium and the bypass medium are mixed.

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 within the cold medium channel.

11. The heat exchange assembly according to claim 10, characterized in that: The bypass channel (2) extends vertically and is located in the center of the shell (1) as a central cylinder; the heat exchange tube (3) in the tube side (102) is spirally wound around the outer periphery of the bypass channel (2).

12. The heat exchange assembly according to claim 11, characterized in that: The bypass channel (2) is equipped with a switch near its outlet end that can cut off or open the passage within the bypass channel (2).

13. The heat exchange assembly according to claim 12, characterized in that: The switching element includes a valve plate (23) and an elastic element (24). The valve plate (23) is rotatably disposed in the bypass channel (2) to cut off or open the passage in the bypass channel (2). The elastic element (24) acts on the valve plate (23) so that the valve plate (23) always has the 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 element (24) and rotate to the state of opening the passage.

14. The heat exchange assembly according to claim 13, characterized in that: The bypass channel (2) has a door plate (25) with a through hole (250) placed horizontally inside. The valve plate (23) is rotatably mounted on the door plate (25) and is located downstream of 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) opens and closes the through hole (250). When the valve plate (23) opens the through hole (250), the passage in the bypass channel (2) is open. 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 panel (25) via a pivot (231), and the elastic element (24) is a torsion spring sleeved on the outer periphery of the pivot (231).

16. The heat exchange assembly according to claim 11, characterized in that: The housing (1) is provided with two tube sheets (5) for supporting the upper and lower ends of the heat exchange tube (3). At least one end of the bypass channel (2) is constrained to the tube sheet (5) in a way that it can move up and down relative to the corresponding tube sheet (5).

17. A hydrogenation system comprising a fractionation tower (200), a stripping tower (300), a heater (400), a high-temperature separation tank (500), and a first heat exchanger (600), characterized in that... It also includes a heat exchange assembly as described 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-temperature separator (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-temperature separator (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 line (310) for conveying the feed of the stripping tower, and the outlet of the cold medium heat exchange channel of the first heat exchange device (600) is connected to the feed inlet 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 fractionation 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 which is connected to the outlet of the third cold medium channel of the third heat exchanger (130), the outlet of which is connected to the input end of the heating furnace (400), and the inlet of which is connected to the outlet at the bottom of the fractionation tower (200).

19. The hydrogenation system according to claim 18, characterized in that: It also includes a third heat exchange device (800), whose inlet of the heat medium heat exchange channel is connected to the outlet of the heat medium heat exchange channel of the second heat exchange device (700), and whose inlet of the 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. 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). 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-temperature gas in the hot medium channel of the first heat exchange device (600).

Images