WO2024066519A1 - 一种用于加氢装置的换热组件及换热工艺 - Google Patents

一种用于加氢装置的换热组件及换热工艺 Download PDF

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Publication number
WO2024066519A1
WO2024066519A1 PCT/CN2023/102257 CN2023102257W WO2024066519A1 WO 2024066519 A1 WO2024066519 A1 WO 2024066519A1 CN 2023102257 W CN2023102257 W CN 2023102257W WO 2024066519 A1 WO2024066519 A1 WO 2024066519A1
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WO
WIPO (PCT)
Prior art keywords
heat exchange
tube
shell
pipeline
water
Prior art date
Application number
PCT/CN2023/102257
Other languages
English (en)
French (fr)
Inventor
陶江
张贤安
王健良
王力
胡兴苗
王艳
徐伟栋
Original Assignee
镇海石化建安工程股份有限公司
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Priority to KR1020247017044A priority Critical patent/KR20240093870A/ko
Publication of WO2024066519A1 publication Critical patent/WO2024066519A1/zh

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/02—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled
    • F28D7/022—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled the conduits of two or more media in heat-exchange relationship being helically coiled, the coils having a cylindrical configuration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D3/00—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium flows in a continuous film, or trickles freely, over the conduits
    • F28D3/02—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium flows in a continuous film, or trickles freely, over the conduits with tubular conduits
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/02—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled
    • F28D7/024—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled the conduits of only one medium being helically coiled tubes, the coils having a cylindrical configuration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F1/00—Tubular elements; Assemblies of tubular elements
    • F28F1/08—Tubular elements crimped or corrugated in longitudinal section
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F11/00—Arrangements for sealing leaky tubes and conduits
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F19/00—Preventing the formation of deposits or corrosion, e.g. by using filters or scrapers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/26—Arrangements for connecting different sections of heat-exchange elements, e.g. of radiators

Definitions

  • the invention belongs to the technical field of heat exchange, and in particular relates to a heat exchange component and a heat exchange process for a hydrogenation device.
  • the temperature of the crude oil is generally higher than that of hydrogen.
  • the temperature of the mixed feed after the two are mixed is higher than the heat of the hot high-fraction gas in the low-temperature section of the heat exchanger, the heat of the hot high-fraction gas in the low-temperature section of the heat exchanger cannot be effectively utilized, resulting in low heat exchange efficiency.
  • the high-pressure air cooler has low cooling efficiency, occupies a large space, has high cost and has many leakage points.
  • the first technical problem to be solved by the present invention is to provide a heat exchange component for a hydrogenation device in view of the current status of the prior art, so as to improve the heat exchange efficiency and reduce the risk of gas-liquid separation.
  • the second technical problem to be solved by the present invention is to provide a heat exchange component for a hydrogenation device to reduce the risk of leakage of hot high-fraction gas.
  • the third technical problem to be solved by the present invention is to provide a heat exchange component for a hydrogenation device to improve the heat exchange effect of an air cooler.
  • the fourth technical problem to be solved by the present invention is to provide a heat exchange process for the above-mentioned heat exchange component.
  • a heat exchange group for a hydrogenation device comprises a first heat exchanger, wherein the first heat exchanger has a vertically arranged shell and a spiral heat exchange tube arranged in the shell and extending vertically, and is characterized in that:
  • a first shell-side inlet pipe is provided at the lower part of the side wall of the shell, a second shell-side inlet pipe is provided at the middle part of the side wall, and a shell-side outlet pipe is provided at the upper part of the side wall, and the first shell-side inlet pipe is connected to a hydrogen pipeline for conveying hydrogen, and the second shell-side inlet pipe is connected to a raw oil pipeline for conveying raw oil;
  • the top of the shell is provided with a tube-side inlet pipe connected to the upper end pipe mouth of the spiral heat exchange tube, and the tube-side inlet pipe is connected to a hot high-fraction gas pipeline for conveying hot high-fraction gas output from the hot high-pressure separation tank of the hydrogenation device.
  • the bottom of the shell is provided with a tube-side outlet pipe connected to the lower end pipe mouth of the spiral heat exchange tube.
  • the “hydrogen” in this application may be the circulating hydrogen output from the hydrogenation device (the circulating hydrogen may contain impurities), or the hydrogen directly connected from the outside.
  • the spiral heat exchange tube can be a single-flow heat exchange tube or a double-flow heat exchange tube, etc.
  • the spiral heat exchange tube is a double-flow heat exchange tube having a first heat exchange tube and a second heat exchange tube, and there are two tube inlet pipes, which are respectively connected to the upper end of the first heat exchange tube and the upper end of the second heat exchange tube;
  • the hot high-pressure gas pipeline includes a main pipeline and two branch pipelines.
  • the input end of the main pipeline is used to connect to the hot high-pressure separation tank of the hydrogenation device.
  • the output end of the main pipeline is simultaneously connected to the input ends of the two branch pipelines.
  • the output ends of the two branch pipelines are respectively connected to the corresponding pipe inlet connecting pipes.
  • each branch pipeline is provided with a first valve for controlling the gas flow rate; at the same time, each branch pipeline is connected to a water injection pipeline for conveying water, and both water injection pipelines are provided with a second valve for controlling the fluid flow rate.
  • first and second valves can be controlled according to actual working conditions.
  • connection point between the water injection pipeline and the branch pipeline is located downstream or upstream of the above-mentioned first valve.
  • there is one pipe outlet connecting pipe which is simultaneously connected to the lower end pipe openings of the first heat exchange pipe and the second heat exchange pipe.
  • the spiral heat exchange tube of the first heat exchanger has a vertically extending spiral section and straight tube sections located on the upper and lower sides of the spiral section;
  • the vertical distance between the second shell side inlet pipe of the first heat exchanger and the lower end of the spiral section is denoted as H1
  • the vertical distance between the upper end and the lower end of the spiral section is denoted as H2, 1/4 ⁇ H1:H2 ⁇ 1/3.
  • first shell-side inlet pipe of the first heat exchanger is located below the lower end of the spiral section, and the shell-side outlet pipe is located above the upper end of the spiral section.
  • a fifth heat exchanger is further included, which has a fifth hot medium channel and a fifth cold medium channel.
  • the end of the fifth heat medium channel is connected to a product pipeline for transporting the reaction product output from the hydrogenation reactor of the hydrogenation device, the output end of the fifth heat medium channel is used to be connected to the input end of the hot high-pressure separation tank of the hydrogenation device, the input end of the fifth cold medium channel is connected to the shell side outlet pipe of the above-mentioned first heat exchanger, and the output end of the fifth cold medium channel is used to be connected to the input end of the hydrogenation reactor.
  • the output end of the fifth cold medium channel is connected to the input end of the hydrogenation reactor through a third pipeline, and further includes a first bypass pipeline, both ends of which are connected to the third pipeline and the raw oil pipeline, and a valve for controlling the flow is provided on the first bypass pipeline.
  • a first bypass pipeline both ends of which are connected to the third pipeline and the raw oil pipeline, and a valve for controlling the flow is provided on the first bypass pipeline.
  • the third pipeline is provided with a heating furnace for heating the fluid medium, and also includes a second bypass pipeline, the input end of the second bypass pipeline is connected to the output end of the fifth cold medium channel, the output end of the second bypass pipeline is used to connect to the input end of the hydrogenation reactor, and the second bypass pipeline and the third pipeline are respectively provided with valves for controlling the flow.
  • the second bypass pipeline can be directly used without using a heating furnace, thereby reducing energy consumption.
  • the heating furnace can be used in the start-up phase (i.e., the phase when the hydrogenation unit is just started).
  • a second heat exchanger is also included, which has a second hot medium channel and a second cold medium channel.
  • the input end of the second hot medium channel is connected to the pipe outlet pipe of the first heat exchanger, and the input end of the second cold medium channel is connected to a cold low-fraction oil pipeline for transporting cold low-fraction oil.
  • a third heat exchanger is also included, having a third hot medium channel and a third cold medium channel, the input end of the third hot medium channel is connected to the output end of the second hot medium channel of the second heat exchanger, and the input end of the third cold medium channel is connected to a water supply pipeline for conveying water.
  • the water in the above water supply pipeline can be low-pressure water or high-pressure water. After heat exchange, low-pressure water can be directly used for household heating, etc. However, since the pressure of low-pressure water is relatively low, the pressure of the hot high-pressure gas exchanged with it is relatively high, and there is a large pressure difference between the two, which leads to the risk of leakage between the cold and hot medium channels of the third heat exchanger and water contamination. Therefore, in order to further solve the above second technical problem, preferably, the water supply pipeline is a pipeline for conveying high-pressure water;
  • It also includes a fourth heat exchanger, which has a fourth hot medium channel and a fourth cold medium channel.
  • the input end of the fourth hot medium channel is connected to the output end of the third cold medium channel of the third heat exchanger, and the input end of the fourth cold medium channel is connected to a low-pressure water pipeline for conveying low-pressure water.
  • the heat exchange between high-pressure water and the hot high-pressure gas in the third hot medium channel can balance the pressure in the third heat exchanger, reducing the risk of pollution due to pressure imbalance.
  • the pressure of high-pressure water is higher than the pressure of hot high-pressure gas, and the high-pressure water is ultimately injected into the hot high-pressure gas, so it does not matter even if the high-pressure water leaks into the hot high-pressure gas.
  • the setting of the fourth heat exchanger can heat the low-pressure water, and the heated low-pressure water can be used for household heating, etc. Even if the high-pressure water in the fourth heat exchanger leaks into the low-pressure water, there is no pollution problem because the medium of both is consistent with water.
  • the output end of the fourth heat medium channel of the fourth heat exchanger is connected to the above-mentioned hot high-gas separation pipeline;
  • the pipe outlet pipe of the first heat exchanger is connected to the input end of the second heat medium channel of the second heat exchanger through a first pipeline, and the first pipeline is connected to the output end of the fourth heat medium channel of the fourth heat exchanger;
  • the output end of the second heat medium channel of the second heat exchanger is connected to the input end of the third heat medium channel of the third heat exchanger through a second pipeline, and the second pipeline is connected to the output end of the fourth heat medium channel of the fourth heat exchanger.
  • the fourth heat exchanger can also be used for water injection of the pipeline for conveying hot high-fraction gas without setting up another water injection pipeline.
  • Water can dissolve some media such as hydrogen sulfide and ammonium salt in the hot high-fraction gas to reduce the phenomenon of some media in the hot high-fraction gas corroding the heat exchanger.
  • an air cooler is also included, whose inlet is connected to the output end of the third heat medium channel of the third heat exchanger, and whose outlet is used to connect to the inlet of the cold high-pressure separation tank of the hydrogenation device.
  • the air cooler comprises:
  • the shell side cylinder is arranged vertically, and has an air inlet and an air outlet at its two ends respectively;
  • Two tube sheets are respectively arranged on the side wall of the shell side cylinder, one above and one below;
  • Two tube boxes are respectively arranged on the corresponding tube plates;
  • a central cylinder is vertically arranged in the shell cylinder
  • a plurality of heat exchange tubes are axially arranged in the shell-side cylinder and spirally wound from the inside to the outside on the outer periphery of the central cylinder to form multiple layers of spiral tubes. Both ends of the heat exchange tubes are respectively supported on corresponding tube sheets and are connected to corresponding tube boxes.
  • a plurality of spray pipes are axially arranged in the shell-side cylinder and are wound in each layer of spiral tubes along the spiral direction of the heat exchange tubes.
  • the pipe opening at the lower end of each spray pipe is a liquid inlet
  • the pipe opening at the upper end of each spray pipe is a liquid outlet opening downward.
  • the liquid outlet is located above the spiral tube and is arranged at intervals along the circumference of the shell-side cylinder.
  • a plurality of spray holes are provided on the tube wall of each spray pipe, and the spray holes are opposite to the tube wall of the adjacent heat exchange tube.
  • each spray pipe is connected to a spray head capable of spraying water downwards.
  • a water collecting tank is provided at the bottom of the shell-side cylinder, and the liquid inlet of the spray pipe is connected to the water collecting tank through a water pump.
  • the air inlet is located at the lower end of the shell-side cylinder, and the air outlet is located at the upper end of the shell-side cylinder.
  • a water collector is further included, which is arranged in the shell cylinder and above the liquid outlet of the above-mentioned spray pipe, and the water collector has a channel for airflow to pass upward and can collect moisture in the airflow. In this way, water consumption can be reduced.
  • the water collector includes a plurality of vertically arranged and connected water collecting plates, and the plurality of water collecting plates are arranged at intervals in the horizontal direction, and the above-mentioned channel is formed between the plate surfaces of two adjacent water collecting plates.
  • a lip extending upward is convexly provided on the plate surface of each water collecting plate, and a water collecting groove with an upward opening and used to collect water accumulated on the plate surface above the lip is formed between the lip and the plate surface of the water collecting plate.
  • the water collector further includes a water collection trough located in the center of the water collector and extending along the arrangement direction of the water collection plate and penetrating the water collection plate, and the water collection ditch extends from the outside to the inside along the plate surface of the water collection plate to the water collection trough and is connected to the water collection trough;
  • the water collector is sleeved on the outer circumference of the above-mentioned central tube, and the water collecting trough is for the central tube to pass through.
  • the interior of the central tube is hollow, and its lower port is connected with the above-mentioned water collecting box.
  • a water inlet connected with the water collecting trough is provided on the tube wall of the central tube opposite to the water collecting trough.
  • the spacing distance between two adjacent water collecting plates is: 20-50 mm.
  • the water collector includes a plurality of vertically arranged and connected water collecting plates, and the plurality of water collecting plates are arranged at intervals in the circumferential direction on the periphery of the central tube, and the above-mentioned channel is formed between the plate surfaces of two adjacent water collecting plates, and a lip extending upward is convexly provided on the plate surface of each water collecting plate, and a water collecting ditch with an upward opening and used to collect moisture in the airflow is formed between the lip and the plate surface of the water collecting plate, and each water collecting ditch extends from the outside to the inside toward the central tube along the plate surface of the water collecting plate, the interior of the central tube is hollow, and its lower port is connected with the above-mentioned water collecting box, and a water inlet is provided on the cylinder wall of the central tube opposite to the water collector, and the water inlet is connected with the above-mentioned water collecting ditch.
  • the water collecting ditch is inclined downward from the outside to the inside.
  • each water collecting plate is made into a wavy structure from top to bottom, and at least one water collecting groove is provided on the same side plate surface of each water collecting plate, and each water collecting groove is located at the protruding part of the plate surface of each water collecting plate.
  • the heat exchange tube can be a smooth tube.
  • the heat exchange tube is a corrugated tube, and has a smooth tube section and a corrugated section with a corrugated surface.
  • the corrugated sections and the smooth tube sections are alternately arranged along the length direction of the heat exchange tube, and the length of the corrugated section is greater than the length of the smooth tube section.
  • the heat exchange tube is a finned tube having a smooth surface of a smooth tube section and a fin section having fins on the surface, wherein the fin section and the smooth tube section are alternately arranged along the length direction of the heat exchange tube, and the length of the fin section is greater than that of the smooth tube section.
  • the two tube sheets and the two tube boxes are grouped together, and there are at least two groups arranged at intervals along the circumference of the shell-side cylinder.
  • the technical solution adopted by the present invention to solve the fourth technical problem is: a heat exchange process using the heat exchange component as described above, characterized by the following steps:
  • the hot high-pressure separation tank outputs hot high-pressure gas with a pressure of 9-11.5MPa and a temperature of 230-250°C into the spiral heat exchange tube of the first heat exchanger through the pipe inlet pipe.
  • the hot high-pressure separation tank outputs hot high-pressure gas with a pressure of 10-12.5MPa and a temperature of 70-95°C.
  • Hydrogen, crude oil with a pressure of 11 to 13.5 MPa and a temperature of 130 to 165°C enter the shell from the first shell inlet pipe and the second shell inlet pipe respectively, and are output from the shell outlet pipe after heat exchange with the hot high-fraction gas in the spiral heat exchange tube.
  • the pressure of the medium output from the shell outlet pipe is 9.7 to 12.2 MPa
  • the temperature is 160 to 180°C
  • the weight percentage of hydrogen in the medium is 6 to 12%.
  • the advantages of the present invention are: since the first shell-side inlet pipe for hydrogen input is arranged at the lower part of the shell side wall, the second shell-side inlet pipe for crude oil input is arranged at the middle part of the shell side wall, and the shell-side outlet pipe is arranged at the upper part of the shell side wall, the hydrogen can first exchange heat with the low-temperature section at the lower part of the spiral heat exchange tube, effectively utilize the heat of the low-temperature section, and recover heat to the maximum extent.
  • the logarithmic mean temperature difference i.e., the temperature difference between the tube-side medium and the shell-side medium
  • the heat exchange area can be reduced, and the equipment cost can be reduced.
  • the hydrogen in the heat exchanger shell is filled below the crude oil.
  • the hydrogen forms an upward lifting force for the crude oil, and the flow rate of the medium in the middle of the shell is generally relatively stable, which is helpful for the distribution of the crude oil.
  • the present application introduces high-pressure water, which exchanges heat with hot high-fraction gas and then exchanges heat with low-temperature water, thereby solving the safety problem caused by leakage of hot high-fraction gas in the prior art and improving the safety of the entire system.
  • the introduced high-pressure water can also be used for water injection into the hot high-fraction gas pipeline.
  • FIG1 is a schematic diagram of the structure of Embodiment 1 of the present invention.
  • FIG2 is an enlarged view of the dotted line frame portion in FIG1 ;
  • FIG3 is a schematic diagram of the structure of Embodiment 2 of the present invention.
  • FIG4 is a schematic diagram of the structure of Embodiment 3 of the present invention.
  • FIG5 is a schematic diagram of the structure of Embodiment 4 of the present invention.
  • FIG6 is a schematic diagram of the structure of Embodiment 5 of the present invention.
  • FIG7 is a schematic diagram of the structure of Embodiment 6 of the present invention.
  • FIG8 is a schematic diagram of the structure of Embodiment 7 of the present invention.
  • FIG9 is a schematic diagram of the structure of Embodiment 8 of the present invention.
  • FIG10 is a schematic diagram of the structure of an air cooler in Example 9 of the present invention.
  • FIG11 is a schematic diagram of the structure between the heat exchange tube and the spray pipe in FIG10 (the cross-sectional area is the water spray area);
  • Fig. 12 is a cross-sectional view taken along the line A-A in Fig. 10;
  • FIG13 is a schematic diagram of the structure between the water collector and the central tube in FIG10;
  • FIG14 is a top view of FIG13
  • FIG15 is a schematic diagram of a partial structure of the central tube in FIG10;
  • FIG16 is a schematic diagram of the structure of the B direction in FIG14;
  • FIG17 is a schematic diagram of a partial structure of the heat exchange tube in FIG10;
  • FIG. 18 is a top view of the water collector and the central tube of the air cooler in Embodiment 10 of the present invention.
  • Embodiment 1 is a diagrammatic representation of Embodiment 1:
  • the heat exchange component includes a first heat exchanger 100 , a second heat exchanger 200 , a third heat exchanger 300 , a fifth heat exchanger 500 and an air cooler 600 .
  • the first heat exchanger 100 has a vertically arranged shell 110 and a spiral heat exchange tube 120 arranged in the shell 110 and extending vertically.
  • a first shell inlet pipe 111 is arranged at the lower part of the side wall of the shell 110, and the first shell inlet pipe 111 is connected to a hydrogen pipeline 130 for transporting hydrogen;
  • a second shell inlet pipe 112 is arranged at the middle part of the side wall of the shell 110, and the second shell inlet pipe 112 is connected to a raw oil pipeline 140 for transporting raw oil;
  • a shell outlet pipe 113 is arranged at the upper part of the side wall of the shell 110.
  • a tube inlet pipe 114 connected to the upper end of the spiral heat exchange tube 120 is arranged at the top of the shell 110, and the tube inlet pipe 114 is connected to a hot high-fraction gas pipeline 150 for transporting hot high-fraction gas output from the hot high-pressure separation tank 700 of the hydrogenation device, and a tube outlet pipe 115 connected to the lower end of the spiral heat exchange tube 120 is arranged at the bottom of the shell 110.
  • the spiral heat exchange tube 120 of the first heat exchanger 100 has a vertically extending spiral section 120a and straight tube sections 120b located on the upper and lower sides of the spiral section 120a; the vertical distance between the second shell inlet pipe 112 of the first heat exchanger 100 and the lower end of the spiral section 120a is denoted as H1, and the vertical distance between the upper and lower ends of the spiral section 120a is denoted as H2, 1/4 ⁇ H1:H2 ⁇ 1/3.
  • the spiral heat exchange tube 120 is a double-flow heat exchange tube having a first heat exchange tube 121 and a second heat exchange tube 122.
  • the pipe inlet pipe 114 has two pipe openings respectively connected to the upper end pipe opening of the first heat exchange tube 121 and the upper end pipe opening of the second heat exchange tube 122.
  • the hot high-gas separation pipeline 150 includes a main pipeline 151 and two branch pipelines 152. The input end of the main pipeline 151 is used to connect to the hot high-pressure separation tank 700 of the hydrogenation device.
  • the output end of the main pipeline 151 is simultaneously connected to the input ends of the two branch pipelines 152.
  • the output ends of the two branch pipelines 152 are respectively connected to the corresponding pipe inlet pipes 114.
  • Each branch pipeline 152 is provided with a first valve 153 for controlling the gas flow rate; at the same time, each branch pipeline 152 is connected to a water injection pipeline 160 for conveying water, and a second valve 161 for controlling the fluid flow rate is provided on both water injection pipelines 160.
  • the connection point between the water injection pipeline 160 and the branch pipeline 152 is located downstream of the first valve 153.
  • the fifth heat exchanger 500 is a vertically arranged single-stream wound tube heat exchanger, having a fifth hot medium channel 510 (shell side of the single-stream wound tube heat exchanger) and a fifth cold medium channel 520 (tube side of the single-stream wound tube heat exchanger).
  • the input end of the fifth hot medium channel 510 is connected to a hydrogenation reactor 710 for transporting hydrogen.
  • the product pipeline 530 of the output reaction product, the output end of the fifth hot medium channel 510 is used to be connected to the input end of the hot high-pressure separation tank 700 of the hydrogenation device, the input end of the fifth cold medium channel 520 is connected to the shell side outlet pipe 113 of the first heat exchanger 100, and the output end of the fifth cold medium channel 520 is used to be connected to the input end of the hydrogenation reactor 710.
  • the output end of the fifth cold medium channel 520 is connected to the input end of the hydrogenation reactor 710 through the third pipeline 540, and a first bypass pipeline 550 is also included, and its two ends are respectively connected to the third pipeline 540 and the raw oil pipeline 140.
  • a valve for controlling the flow is provided on the first bypass pipeline 550.
  • the third pipeline 540 is provided with a heating furnace 560 for heating the fluid medium, and also includes a second bypass pipeline 570, the input end of the second bypass pipeline 570 is connected to the output end of the fifth cold medium channel 520 of the fifth heat exchanger 500, and the output end of the second bypass pipeline 570 is used to connect to the input end of the hydrogenation reactor 710.
  • the second bypass pipeline 570 and the third pipeline 540 are both provided with valves for controlling the flow rate.
  • the second heat exchanger 200 is a vertically arranged single-stream wound tube heat exchanger having a second hot medium channel 210 (the tube side of the single-stream wound tube heat exchanger) and a second cold medium channel 220 (the shell side of the single-stream wound tube heat exchanger).
  • the input end of the second hot medium channel 210 is connected to the tube side outlet pipe 115 of the first heat exchanger 100 via a first pipeline 240 (the first pipeline 240 is connected to a pipeline for supplying high-pressure water), and the input end of the second cold medium channel 220 is connected to a cold low-separation oil pipeline 230 for conveying cold low-separation oil.
  • the third heat exchanger 300 is a vertically arranged single-flow wound tube heat exchanger having a third heat medium channel 310 (the tube side of the single-flow wound tube heat exchanger) and a third cold medium channel 320 (the shell side of the single-flow wound tube heat exchanger).
  • the input end of the third heat medium channel 310 is connected to the output end of the second heat medium channel 210 of the second heat exchanger 200 through a second pipeline 340 (the second pipeline 340 is connected to a pipeline for supplying high-pressure water), and the input end of the third cold medium channel 320 is connected to a water supply pipeline 330 for conveying water.
  • the air cooler 600 is an existing high-pressure air cooler, whose inlet is connected to the output end of the third heat medium channel 310 of the third heat exchanger 300, and whose outlet is used to connect to the inlet of the cold high-pressure separation tank 720 of the hydrogenation device.
  • the heat exchange assembly of this embodiment is used for a hydrogenation device, which has a hot high-pressure separation tank 700, a hydrogenation reactor 710, a cold high-pressure separation tank 720, a cold low-pressure separation tank 730, and a hot low-pressure separation tank 740.
  • the top outlet of the hot high-pressure separation tank 700 is connected to the pipe inlet pipe 114 of the first heat exchanger 100 in the heat exchange assembly through the hot high-pressure gas pipeline 150, the bottom outlet of the hot high-pressure separation tank 700 is connected to the inlet of the hot low-pressure separation tank 740 through a pipeline (a pressure reducing device is provided on the pipeline), and the top outlet of the hot low-pressure separation tank 740 is connected to the inlet of the cold low-pressure separation tank 730 through a pipeline (a hot low-pressure gas air cooler is provided on the pipeline).
  • the inlet of the cold high-pressure separation tank 720 is connected to the outlet of the air cooler 600 in the heat exchange assembly, and the bottom outlet of the cold high-pressure separation tank 720 is connected to the inlet of the cold low-pressure separation tank 730 through a pipeline (a pressure reducing device is provided on the pipeline).
  • the top outlet of the cold high-pressure separation tank 720 is connected to a circulating pump through a pipeline (a circulating hydrogen desulfurization tower and a compressor buffer tank are arranged in sequence along the fluid flow direction of the pipeline).
  • the fluid output by the circulating pump is divided into two paths. The first path goes through the above-mentioned hydrogen pipeline 130, and the second path is transported to the hydrogenation reactor 710.
  • Embodiment 2 is a diagrammatic representation of Embodiment 1:
  • FIG3 it is a preferred embodiment 2 of a heat exchange assembly for a hydrogenation device of the present invention.
  • This embodiment is basically the same as the embodiment 1, except that in this embodiment, the second and third heat exchangers are combined into a vertical heat exchanger, and the second heat exchanger 200 is located above the third heat exchanger 300.
  • the fifth heat exchanger 500 and the first heat exchanger 100 are combined into a vertical heat exchanger, and the fifth heat exchanger 500 is located above the first heat exchanger 100, and the two are separated by a tube sheet.
  • the lower end of the fifth cold medium channel 520 of the fifth heat exchanger 500 is supported on the tube sheet and communicated with the hollow inside the shell 110 of the first heat exchanger 100.
  • Embodiment 3 is a diagrammatic representation of Embodiment 3
  • This embodiment is basically the same as the embodiment 1, except that in this embodiment, the first, second, and third heat exchangers are combined into a vertical heat exchanger, and the first heat exchanger 100, the second heat exchanger 200, and the third heat exchanger 300 are arranged sequentially from top to bottom.
  • Embodiment 4 is a diagrammatic representation of Embodiment 4:
  • This embodiment is basically the same as the embodiment 1, except that in this embodiment, the first, second, third, and fifth heat exchangers are combined into a vertical heat exchanger, and the fifth heat exchanger 500, the first heat exchanger 100, the second heat exchanger 200, and the third heat exchanger 300 are arranged in sequence from top to bottom.
  • Embodiment 5 is a diagrammatic representation of Embodiment 5:
  • FIG6 it is a preferred embodiment 5 of a heat exchange component for a hydrogenation device of the present invention.
  • This embodiment is basically the same as the embodiment 1, except that the water supply pipeline 330 on the third heat exchanger 300 in this embodiment is a pipeline for conveying high-pressure water; the heat exchange component of this embodiment also includes a fourth heat exchanger 400, which is a vertically arranged single-stream wound tube heat exchanger, having a fourth hot medium channel 410 (which is the tube side of the single-stream wound tube heat exchanger) and a fourth cold medium channel 420 (which is the shell side of the single-stream wound tube heat exchanger), the input end of the fourth hot medium channel 410 is connected to the output end of the third cold medium channel 320 of the third heat exchanger 300, and the input end of the fourth cold medium channel 420 is connected to a low-pressure water pipeline 430 for conveying low-pressure water.
  • a fourth heat exchanger 400 which is a vertically arranged single-stream wound tube heat exchanger, having a fourth hot medium channel 410
  • the output end of the fourth heat medium channel 410 of the fourth heat exchanger 400 is simultaneously connected to the above-mentioned hot high-pressure gas pipeline 150, the first pipeline 240 and the second pipeline 340. That is, in this embodiment, the high-pressure water output from the output end of the fourth heat medium channel 410 can supply water to the hot high-pressure gas pipeline 150, the first pipeline 240 and the second pipeline 340, so that the hot high-pressure gas pipeline 150, the first pipeline 240 and the second pipeline 340 do not need to be connected to high-pressure water.
  • the spiral heat exchange tube of the first heat exchanger 100 is a single-flow heat exchange tube.
  • the first heat exchanger 100 has only one tube-side inlet pipe 114, which is directly connected to the outlet at the top of the hot high-pressure separation tank 700 through a hot high-gas separation pipeline 150.
  • the first shell inlet pipe 111 of the first heat exchanger 100 is located at the lower end of the spiral section 120a.
  • the shell side outlet pipe 113 is located above the upper end of the spiral section 120a.
  • the hot high-pressure separation tank 700 outputs a hot high-fraction gas with a pressure of 9-11.5 MPa and a temperature of 230-250°C into the spiral heat exchange tube 120 of the first heat exchanger 100 through the tube side inlet pipe 114.
  • the hydrogen with a pressure of 10-12.5 MPa and a temperature of 70-95°C and the feedstock oil with a pressure of 11-13.5 MPa and a temperature of 130-165°C enter the shell 110 from the first shell side inlet pipe 111 and the second shell side inlet pipe 112 respectively, and are output from the shell side outlet pipe 113 after heat exchange with the hot high-fraction gas in the spiral heat exchange tube 120.
  • the medium output from the shell side outlet pipe 113 has a pressure of 9.7-12.2 MPa and a temperature of 160-180°C, and the weight percentage of hydrogen in the medium is 6-12%;
  • the hot high fraction gas outputted from the outlet pipe 115 of the first heat exchanger 100 enters the second heat medium channel 210 of the second heat exchanger 200, and exchanges heat with the cold low fraction oil in the second cold medium channel 220.
  • the pressure of the cold low fraction oil before entering the second cold medium channel 220 is 1.0-1.8 MPa, and the temperature is 48-55°C.
  • the pressure of the cold low fraction oil exiting the second cold medium channel 220 is 1.0-1.8 MPa, and the temperature is 160-185°C.
  • the hot high-fraction gas output from the second heat medium channel 210 of the second heat exchanger 200 enters the third heat medium channel 310 of the third heat exchanger 300, and exchanges heat with the high-pressure water in the third cold medium channel 320, wherein the pressure of the high-pressure water before entering the third cold medium channel 320 is 12.5-13.5 MPa and the temperature is 60-75°C; the temperature of the hot high-fraction gas output from the third heat medium channel 310 is 70-80°C;
  • the high-pressure water output from the third cold medium channel 320 enters the fourth hot medium channel 410 of the fourth heat exchanger 400, and exchanges heat with the low-pressure water in the fourth cold medium channel 420, wherein the pressure of the low-pressure water before entering the fourth cold medium channel 420 is 0.6-1.2 MPa and the temperature is 60-70°C, and the pressure of the low-pressure water out of the fourth cold medium channel 420 after heat exchange is 0.6-1.2 MPa and the temperature is 95-135°C;
  • the medium output from the shell outlet pipe 113 of the first heat exchanger 100 enters the fifth cold medium channel 520 of the fifth heat exchanger 500, exchanges heat with the heat medium in the fifth heat medium channel 510, and then is output from the fifth heat exchanger 500 (output pressure is 9.5-12.0 MPa, temperature is 320-365°C), and then selectively goes through the third pipeline 540 or the second bypass pipeline 570, and then enters the hydrogenation reactor 710 for hydrogenation reaction.
  • the pressure of the medium before entering the hydrogenation reactor 710 is 9.5-12.0 MPa, and the temperature is 335-380°C; the pressure of the reaction product output from the hydrogenation reactor 710 is 9.2-11.6 MPa, and the temperature is 360-415°C, and then enters the fifth heat medium channel 510 of the fifth heat exchanger 500, and the reaction product output from the fifth heat exchanger 500 enters the hot high-pressure separation tank 700 for gas-liquid separation.
  • Embodiment 6 is a diagrammatic representation of Embodiment 6
  • FIG7 it is a preferred embodiment 6 of a heat exchange assembly for a hydrogenation device of the present invention, which is basically the same as the embodiment 5, except that the fifth heat exchanger 500 and the first heat exchanger 100 are combined into a vertical heat exchanger in the present embodiment, and the fifth heat exchanger 500 is located above the first heat exchanger 100.
  • the structure of the first heat exchanger 100 in the present embodiment is basically the same as the structure of the first heat exchanger 100 in the embodiment 1.
  • Embodiment 7 is a diagrammatic representation of Embodiment 7:
  • FIG8 it is a preferred embodiment 7 of a heat exchange assembly for a hydrogenation device of the present invention.
  • This embodiment is basically the same as the embodiment 5, except that the first, second and third heat exchangers in this embodiment are combined into a vertical heat exchanger, and the first heat exchanger 100, the second heat exchanger 200 and the third heat exchanger 300 are arranged from top to bottom in sequence.
  • the structure of the first heat exchanger 100 in this embodiment is basically the same as the structure of the first heat exchanger 100 in the embodiment 1.
  • Embodiment 8 is a diagrammatic representation of Embodiment 8
  • FIG9 it is a preferred embodiment 8 of a heat exchange component for a hydrogenation device of the present invention.
  • This embodiment is basically the same as the embodiment 5, except that in this embodiment, the first, second, third and fifth heat exchangers are combined into a vertical heat exchanger, and the fifth heat exchanger 500, the first heat exchanger 100, the second heat exchanger 200 and the third heat exchanger 300 are arranged in sequence from top to bottom.
  • the structure of the first heat exchanger 100 in this embodiment is basically the same as the structure of the first heat exchanger 100 in Example 1, the difference is that in this embodiment: along the flow direction of the hot high-fraction gas in the branch pipeline 152, the connection point between the water injection pipeline 160 and the branch pipeline 152 is located upstream of the above-mentioned first valve 153.
  • Embodiment 9 is a diagrammatic representation of Embodiment 9:
  • FIGS. 10 to 17 a preferred embodiment 9 of a heat exchange assembly for a hydrogenation device of the present invention is shown.
  • This embodiment is basically the same as the embodiment 1, except that the structure of the air cooler 600 in this embodiment is different, as follows:
  • the air cooler 600 of this embodiment is a wound tube composite air cooler, which includes a shell-side cylinder 1, two tube sheets, two tube boxes 2, a central tube 3, multiple heat exchange tubes 4, multiple spray pipes 5, a water collecting box 6, a water pump 7, and a water collector 8.
  • the shell-side cylinder 1 is arranged vertically, with an air inlet 11 at its lower end and an air outlet 12 at its upper end, and a fan is arranged at the air outlet 12, so that air flows into the shell-side cylinder 1 from the air inlet 11 and then is discharged from the air outlet 12.
  • a water collecting tank 6 is arranged at the bottom of the shell-side cylinder 1.
  • Two tube sheets are disposed one above and one below on the side wall of the shell-side cylinder 1 ; two tube boxes 2 are disposed on the corresponding tube sheets respectively and serve as the inlet and outlet of the air cooler 600 .
  • the central tube 3 is vertically arranged in the shell side cylinder 1.
  • the interior of the central tube 3 is hollow, and its lower port 31 extends into the water collecting box 6.
  • a plurality of heat exchange tubes 4 are axially arranged in the shell cylinder 1, and are spirally wound from the inside to the outside on the outer periphery of the central cylinder 3 to form multiple layers of spiral tubes.
  • the spacing between adjacent layers of spiral tubes is not less than 4 mm.
  • the two ends of the heat exchange tube 4 are respectively supported on their corresponding tube sheets and are connected to the corresponding tube box 2.
  • the heat exchange tube 4 is a corrugated tube, and has a smooth tube section 41 and a corrugated section 42 with a corrugated surface.
  • the corrugated section 42 and the smooth tube section 41 are alternately arranged along the length direction of the heat exchange tube 4, and the length of the corrugated section 42 is greater than the length of the smooth tube section 41; specifically, the length of the corrugated section 42 is 200 mm, and the length of the smooth tube section 41 is 50 mm.
  • the smooth tube section 41 is used to connect with a fixing (such as a gasket for a heat exchanger) Fitting is performed to fix the heat exchange tube.
  • a plurality of spray pipes 5 are axially arranged in the shell-side cylinder 1, and are wound in each layer of spiral tubes along the spiral direction of the heat exchange tube 4 (there is at least one spray pipe 5 in each layer of spiral tubes, and this spray pipe 5 is wound synchronously with the plurality of heat exchange tubes 4 in this layer, see FIG2 ), and the pipe mouth at the lower end of each spray pipe 5 is a liquid inlet 51, and is connected to the water collecting tank 6 through a water pump 7.
  • the pipe mouth at the upper end of each spray pipe 5 is a liquid outlet 52 opening downward, and the liquid outlet 52 is located above the spiral tube and is arranged at equal intervals along the circumference of the shell-side cylinder 1.
  • each spray pipe 5 is connected to a nozzle 54 that can spray water downward.
  • the three adjacent nozzles 54 are distributed with three end points of an equilateral triangle to ensure that the spray radius of each nozzle 54 is not less than 150 mm.
  • a plurality of spray holes 53 are also provided on the tube wall of each spray pipe 5, and the spray holes 53 are opposite to the tube wall of the adjacent heat exchange tube 4 to spray the adjacent heat exchange tube.
  • the multi-layer spiral tube is sequentially recorded as the first layer, the second layer, ..., and the Nth layer from the inside to the outside, and the plurality of spray holes of the spray pipe in the first layer are respectively oriented toward the upper surface of the heat exchange tube in the second layer and the adjacent heat exchange tube in the first layer (located below the spray pipe in the first layer); the plurality of spray holes of the spray pipe in the Nth layer are respectively oriented toward the upper surface of the heat exchange tube in the N-1th layer and the adjacent heat exchange tube in the Nth layer (located below the spray pipe in the Nth layer); the plurality of spray holes of the spray pipe in the intermediate layer between the first layer and the Nth layer are respectively oriented toward the upper surface of the heat exchange tube in the adjacent layer and the adjacent heat exchange tube in the same layer.
  • the water collector 8 is arranged in the shell cylinder 1 and is located above the liquid outlet 52 of the spray pipe 5, and the water collector 8 has a channel 80 for air flow to pass upward and collect moisture in the air flow.
  • the water collector 8 is sleeved on the outer periphery of the central cylinder 3, and includes a plurality of vertically arranged and connected water collecting plates 81.
  • the plurality of water collecting plates 81 can be connected through an upper base plate and/or a lower base plate (the upper and lower base plates can be made into a grid shape, or a plate with holes); they can also be connected through connecting rods, and each connecting rod passes through each water collecting plate 81 in turn to connect each water collecting plate 81.
  • a plurality of water collecting plates 81 are arranged in a horizontal direction at intervals.
  • the interval between two adjacent water collecting plates is 20 to 50 mm (the interval can be 20 mm, 50 mm or any value therebetween).
  • Such a design can ensure the air-water separation effect without affecting the heat exchange of the air cooler, so that the above-mentioned channel 80 is formed between the plate surfaces of two adjacent water collecting plates 81.
  • a lip 811 extending upward is convexly provided on the plate surface of each water collecting plate 81, and a water collecting ditch 82 with an upward opening and used to collect water accumulated on the plate surface above the lip 811 is formed between the lip 811 and the plate surface of the water collecting plate 81.
  • each water collecting plate 81 is represented by a baseline a, and the number of baselines a is not limited to the number shown in the figure. In the figure, several baselines a are used to represent the installation position and arrangement direction of the water collecting plate 81).
  • the water collector 8 also includes a water collecting trough 83 located in the center of the water collector 8 and extending along the arrangement direction of the water collecting plate 81 and penetrating the water collecting plate 81.
  • the water collecting trough 83 is a structure having a bottom plate and side plates located on both sides of the bottom plate. The bottom plate and the two side plates form a water collecting trough 83 with a U-shaped cross section.
  • the water collecting ditch 82 extends from the outside to the inside along the plate surface of the water collecting plate 81 to the water collecting trough 83 and is connected to the water collecting trough 83, and the water collecting ditch 82 is inclined downward from the outside to the inside so that the water in the water collecting ditch 82 can flow to the water collecting trough 83 under the action of its own gravity.
  • the above-mentioned central tube 3 passes through the water collecting trough 83, and the tube wall of the central tube 3 opposite to the water collecting trough 83 is provided with a water inlet 32, and the water inlet 32 is connected to the above-mentioned water collecting trough 83. In this way, the water collected in the water collecting ditch 82 can enter the central tube 3 through the water collecting trough 83 and the water inlet 32, and then flow back to the water collecting box 6, thereby realizing Reuse of cooling water.
  • each of the above-mentioned water collection plates 81 is made into a wavy structure from top to bottom, please refer to Figure 7.
  • One or more water collection grooves 82 can be designed on the same side surface of each water collection plate 81 as needed, and each water collection groove 82 is located at the protruding part of the plate surface of each water collection plate 81, so that the water vapor accumulated on the plate surface of each water collection plate 81 can be completely collected by the water collection groove 82 when flowing downstream.
  • Embodiment 10 is a diagrammatic representation of Embodiment 10:
  • the water collector 8 of this embodiment includes a plurality of vertically arranged and connected water collecting plates 81, and the plurality of water collecting plates 81 are arranged circumferentially at intervals on the periphery of the central tube 3, and a channel 80 for air to pass upward is formed between the plate surfaces of two adjacent water collecting plates 81, and an upwardly extending lip 811 is convexly provided on the plate surface of each water collecting plate 81, and a water collecting ditch 82 with an upward opening and used to collect water stored in the plate area above the lip 811 is formed between the lip 811 and the plate surface of the water collecting plate 81, and each water collecting ditch 82 extends from the outside to the inside toward the central tube 3 along the plate surface of the water collecting plate 81, and the water collecting
  • the interior of the central tube 3 is hollow, and its lower port 31 is connected to the water collecting box 6 .
  • a water inlet 32 is provided on the tube wall of the central tube 3 opposite to the water collector 8 , and the water inlet 32 is connected to the water collecting ditch 82 .
  • the moisture in the air flow will accumulate on the surface of the water collecting plate 81 and flow downward along the surface of the water collecting plate 81 into the water collecting ditch 82.
  • the water in the water collecting ditch 82 flows along the water collecting ditch 82 to the water inlet 32 of the central tube 3, and then flows back to the water collecting tank 6 through the central tube 3, thereby realizing the recycling and reuse of water.

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Abstract

一种用于加氢装置的换热组件，包括有第一换热器，第一换热器具有竖向设置的壳体以及设于壳体内并竖向延伸的螺旋换热管，壳体的侧壁的下部设有第一壳程入口接管，侧壁的中部设有第二壳程入口接管，侧壁的上部设有壳程出口接管，且第一壳程入口接管连接有用于输送氢气的氢气管线，第二壳程入口接管连接有用于输送原料油的原料油管线；壳体的顶部设有与螺旋换热管的上端管口相连通的管程入口接管，管程入口接管连接有用于输送加氢装置之热高压分离罐输出的热高分气的热高分气管线，壳体的底部设有与螺旋换热管的下端管口相连通的管程出口接管。本申请还公开了换热组件的换热工艺。与现有技术相比，本申请能提高换热效率。

Description

一种用于加氢装置的换热组件及换热工艺 技术领域
本发明属于热交换技术领域，具体涉及一种用于加氢装置的换热组件及换热工艺。
背景技术
现有的加氢装置如申请号为CN202110477804.0的发明专利申请《采用多股流缠绕管式换热器的加氢换热***及换热工艺》(申请公开号为CN113063309A)、申请号为CN202110477849.8的发明专利申请《采用多股流缠绕管式换热器的加氢换热***及换热工艺》(申请公开号为CN113091498A)公开的方案，反应用的原料油与氢气混合后输入换热器内，与热高分气进行换热，以提高原料油和氢气的温度。
现有技术中原料油与氢气混合后的换热存在如下待解决的技术问题：
1、原料油与氢气混合后从底部进入换热器内，换热器底部的流速较低，且原料油为液相，氢气为气相，液相比重明显大于气相比重，会造成气液分离，最终在设备底部出现大量积液的问题；
2、原料油的温度一般高于氢气的温度，当两者混合后的混合进料的温度高于换热器内低温段的热高分气的热量时，则无法有效利用换热器内低温段的热高分气的热量，使得换热效率较低。
并且现有的用于加氢装置的换热组件存在如下技术问题：
1、高压的热高分气与低压热水换热，存在热高分气泄漏至低压热水的情况，对后续水***及公用工程***带来安全隐患；
2、高压空冷器的冷却效率低、占用空间大、成本高且存在泄漏点多等问题。
发明内容
本发明所要解决的第一个技术问题是针对现有技术的现状，提供一种用于加氢装置的换热组件，以提高换热效率的同时降低气液分离的风险。
本发明所要解决的第二个技术问题是提供一种用于加氢装置的换热组件，以降低热高分气泄漏的风险。
本发明所要解决的第三个技术问题是提供一种用于加氢装置的换热组件，以提高空冷器的换热效果。
本发明所要解决的第四个技术问题是提供一种上述换热组件的换热工艺。
本发明解决上述第一个技术问题所采用的技术方案为：一种用于加氢装置的换热组 件，包括有第一换热器，所述第一换热器具有竖向设置的壳体以及设于壳体内并竖向延伸的螺旋换热管，其特征在于：
所述壳体的侧壁的下部设有第一壳程入口接管，侧壁的中部设有第二壳程入口接管，侧壁的上部设有壳程出口接管，且所述第一壳程入口接管连接有用于输送氢气的氢气管线，所述第二壳程入口接管连接有用于输送原料油的原料油管线；
同时所述壳体的顶部设有与螺旋换热管的上端管口相连通的管程入口接管，所述管程入口接管连接有用于输送加氢装置之热高压分离罐输出的热高分气的热高分气管线，所述壳体的底部设有与螺旋换热管的下端管口相连通的管程出口接管。
本申请中的“氢气”可为从加氢装置输出的循环氢(循环氢中可能带有杂质)，或者是直接从外部接入的氢气。
为提高换热效果，优选地，上述螺旋换热管可为单股流换热管或双股流换热管等，优选地，所述螺旋换热管为具有第一股换热管和第二股换热管的双股流换热管，所述管程入口接管有两个，分别与第一股换热管的上端管口、第二股换热管的上端管口相连通；
所述热高分气管线包括有主路管线和两个支路管线，所述主路管线的输入端用于连接至加氢装置之热高压分离罐，所述主路管线的输出端同时与两个支路管线的输入端相连通，所述两个支路管线的输出端分别与对应的管程入口接管相连通。
优选地，每个所述支路管线上均设有用于控制气体流量的第一阀门；同时，每个支路管线均连接有用于输送水的注水管线，两个注水管线上均设有用于控制流体流量的第二阀门。如此，可根据实际工况控制第一、第二阀门的启闭。
进一步地，沿热高分气在支路管线内的流动方向，所述注水管线与支路管线的连通处位于上述第一阀门的下游或上游。
优选地，所述管程出口接管为一个，并同时与上述第一股换热管、第二股换热管的下端管口相连通。
为提高换热效率，优选地，所述第一换热器之螺旋换热管具有竖向延伸的螺旋段以及位于螺旋段上下两侧的直管段；
记第一换热器之第二壳程入口接管与所述螺旋段的下端部之间的竖直距离为H1，记所述螺旋段的上端部、下端部之间的竖直距离为H2，1/4≤H1:H2≤1/3。
即若第二壳程入口接管所处的位置过高，会影响原料油与换热管内介质的换热，若第二壳程入口接管所处的位置过低，可能存在气液分离的问题；本申请中1/4≤H1:H2≤1/3，能保证换热效率的同时，又能较好地降低气液分离的风险。
进一步地，所述第一换热器之第一壳程入口接管位于所述螺旋段之下端部的下方，所述壳程出口接管位于所述螺旋段之上端部的上方。
在上述方案中，为提高加氢反应器的进料温度，提高能源的利用率，优选地，还包括有第五换热器，具有第五热介质通道和第五冷介质通道，所述第五热介质通道的输入 端连接有用于输送加氢装置之加氢反应器输出的反应产物的产物管线，所述第五热介质通道的输出端用于连接至加氢装置之热高压分离罐的输入端，所述第五冷介质通道的输入端与上述第一换热器之壳程出口接管相连通，所述第五冷介质通道的输出端用于连接至加氢反应器的输入端。
优选地，所述第五冷介质通道的输出端与加氢反应器的输入端之间通过第三管线相连通，还包括有第一旁路管线，其两端分别与所述第三管线以及原料油管线相连通，且第一旁路管线上设有用于控制流量的阀门。如此，当第五冷介质通道的输出端输出的介质温度较高时，可通过打开第一旁路管线，引入低温的原料油来调节温度。
进一步地，所述第三管线上设有用于加热流体介质的加热炉，还包括有第二旁路管线，所述第二旁路管线的输入端与上述第五冷介质通道的输出端相连通，所述第二旁路管线的输出端用于连接至加氢反应器的输入端，且所述第二旁路管线以及第三管线上分别设有用于控制流量的阀门。当第五冷介质通道的输出端输出的介质温度达到加氢反应器的进料温度时，可直接走第二旁路管线，而无需另外使用加热炉，从而降低能源的消耗。加热炉可在开工阶段(即刚开始运行加氢装置的阶段)使用。
在上述各方案中，为进一步利用第一换热器换热后的热高分气的热量，还包括有第二换热器，具有第二热介质通道和第二冷介质通道，所述第二热介质通道的输入端与上述第一换热器之管程出口接管相连通，所述第二冷介质通道的输入端连接有用于输送冷低分油的冷低分油管线。
优选地，还包括有第三换热器，具有第三热介质通道和第三冷介质通道，所述第三热介质通道的输入端与上述第二换热器之第二热介质通道的输出端相连通，所述第三冷介质通道的输入端连接有用于输送水的供水管线。
以上供水管线中的水可为低压水或高压水，低压水换热后可直接用于家庭供暖等，但由于低压水的压力较低，与其换热的热高分气的压力较大，两者存在较大的压力差，从而导致第三换热器的冷热介质通道之间存在泄露而污染水的风险，故而，为了进一步解决上述第二个技术问题，优选地，所述供水管线为用于输送高压水的管线；
还包括有第四换热器，具有第四热介质通道和第四冷介质通道，所述第四热介质通道的输入端与上述第三换热器之第三冷介质通道的输出端相连通，所述第四冷介质通道的输入端连接有用于输送低压水的低压水管线。如此，高压水与第三热介质通道内的热高分气换热能使得第三换热器内压力平衡，降低因压力失衡而污染的风险，具体地，高压水的压力高于热高分气的压力，且高压水最终是要注入热高分气，就算高压水泄漏至热高分气中也没有关系。即高压水不论泄漏至热高分气还是低压水中均不会造成污染。且第四换热器的设置能实现加热低压水，加热后的低压水能用于家庭供热等；且第四换热器内即使高压水泄漏至低压水，因两者的介质一致均为水，故而也不存在污染的问题。
优选地，所述第四换热器之第四热介质通道的输出端与上述热高分气管线相连通；
所述第一换热器之管程出口接管与所述第二换热器之第二热介质通道的输入端之间通过第一管线相连通，该第一管线与所述第四换热器之第四热介质通道的输出端相连通；
所述第二换热器之第二热介质通道的输出端与第三换热器之第三热介质通道的输入端之间通过第二管线相连通，该第二管线与所述第四换热器之第四热介质通道的输出端相连通。
从而使得第四换热器的设置还能用于输送热高分气的管线的注水，而无需另外设置注水管线。水能溶解热高分气中的硫化氢、铵盐等部分介质，以降低热高分气中的部分介质腐蚀换热器的现象出现。
优选地，还包括有空冷器，其入口与上述第三换热器之第三热介质通道的输出端相连通，其出口用于连接至加氢装置之冷高压分离罐的入口。
为进一步解决上述第三个技术问题，优选地，所述空冷器包括有：
壳程筒体，竖向设置，其两个端部分别具有进风口、出风口；
两个管板，分别一上一下设于所述壳程筒体的侧壁上；
两个管箱，分别设于各自对应的管板上；
中心筒，竖向设于所述壳程筒体内；
多根换热管，沿轴向设于所述壳程筒体内，且由内而外螺旋缠绕在所述中心筒的外周而成多层螺旋管，所述换热管的两端分别支撑于各自对应的管板上并与对应的管箱相连通；
多根喷淋管，沿轴向设于所述壳程筒体内，且沿着换热管的螺旋方向缠绕在各层螺旋管中，各喷淋管下端的管口为进液口，各喷淋管上端的管口为开口朝下的出液口，且出液口位于所述螺旋管上方，并沿着壳程筒体的周向间隔布置；同时，各所述喷淋管的管壁上均设有多个喷淋孔，所述喷淋孔与相邻的换热管的管壁相对。
如此，当空冷器工作时，喷淋管内部通冷却液，冷却液从进液口进入喷淋管内，部分冷却液通过喷淋孔喷至相邻的换热管，部分冷却液从出液口向下喷出，实现对换热管内高温热介质的换热，且周向间隔布置的出液口能保证均匀喷水，且喷水量稳定，进而能有效提高换热效率。
优选地，各喷淋管上端的管口连接有能向下喷水的喷头。
在上述方案中，优选地，所述壳程筒体的底部设有集水箱，所述喷淋管的进液口通过水泵与集水箱相连通。
进一步地，所述进风口位于壳程筒体的下端部、所述出风口位于壳程筒体的上端部。
为提高集水箱内水的利用率，优选地，还包括有集水器，设于所述壳程筒体内并位于上述喷淋管之出液口的上方，且该集水器具有供气流向上通过、并能收集气流中水分的通道。如此能降低水的消耗。
较优选地，所述集水器包括有多个竖向设置并相连接的集水板，多个集水板沿水平方向间隔排列，相邻两个集水板的板面之间形成上述通道，同时，各集水板的板面上凸设有向上延伸的唇片，所述唇片与集水板的板面之间形成开口朝上并用于收集该唇片之上的板面上积存水分的集水沟。
为了能较好地回收集水沟内的水，进一步地，所述集水器还包括有位于集水器的中央并沿集水板的排列方向延伸而贯穿集水板的集水槽，所述集水沟沿集水板的板面由外至内向集水槽延伸并与集水槽相连通；
所述集水器套设在上述中心筒的外周，且集水槽供中心筒穿过，所述中心筒的内部中空，且其下端口与上述集水箱相连通，中心筒之与集水槽相对的筒壁上设有与集水槽相连通的入水口。
为了能保证气水分离效果的同时，还不影响空冷器的换热，优选地，相邻两个集水板之间的间隔距离为：20～50mm。
为了能较好地收集集水沟内的水，同样优选地，所述集水器包括有多个竖向设置并相连接的集水板，多个集水板沿周向间隔排列在中心筒的***，相邻两个集水板的板面之间形成上述通道，各集水板的板面上凸设有向上延伸的唇片，所述唇片与集水板的板面之间形成开口朝上并用于收集气流中水分的集水沟，各集水沟沿集水板的板面由外至内向中心筒延伸，所述中心筒的内部中空，且其下端口与上述集水箱相连通，中心筒之与集水器相对的筒壁上设有入水口，该入水口与上述集水沟相连通。
为利于集水沟内的水能较好地流动至集水箱，优选地，所述集水沟由外至内向下倾斜。
为了提高气水分离效果，且能较好地收集水分，优选地，各集水板均自上而下制成波浪状的结构，各集水板的同一侧板面上设有至少一个上述集水沟，且各集水沟位于各集水板之板面的外突部位处。
在上述各方案中，换热管可为表面光滑的光管，为提高换热效果，优选地，所述换热管为波纹管，并具有表面光滑的光管段和表面具有波纹的波纹段，所述波纹段与光管段沿换热管的长度方向交替布置，且波纹段的长度大于光管段的长度；
或，所述换热管为翅片管，并具有表面光滑的光管段和表面具有翅片的翅片段，所述翅片段与光管段沿换热管的长度方向交替布置，且翅片段的长度大于光管段的长度。
优选地，以上述的两个管板以及两个管箱为一组，有至少两组并沿壳程筒体的周向间隔布置。当然也可仅有一组，具体根据换热管的数量进行设计。
本发明解决上述第四个技术问题所采用的技术方案为：一种采用如上所述的换热组件的换热工艺，其特征在于步骤如下：
热高压分离罐输出的压力为9～11.5MPa、温度为230～250℃的热高分气通过管程入口接管进入第一换热器的螺旋换热管内，同时，压力为10～12.5MPa、温度为70～95℃的 氢气，压力为11～13.5MPa、温度为130～165℃的原料油分别从第一壳程入口接管、第二壳程入口接管进入壳体内，与螺旋换热管内的热高分气进行换热后从壳程出口接管输出，且从壳程出口接管输出的介质的压力为9.7～12.2MPa，温度为160～180℃，且介质中氢气的重量百分比为6～12％。
与现有技术相比，本发明的优点在于：由于将供氢气输入的第一壳程入口接管设于壳体侧壁的下部，将供原料油输入的第二壳程入口接管设于壳体侧壁的中部，将壳程出口接管设于壳体侧壁的上部，使得氢气能先与螺旋换热管下部的低温段进行换热，有效利用低温段热量，最大限度的回收热量，同时可增大对数平均温差(即管程介质与壳程介质之间的温差)，减小换热面积，降低设备成本。
同时，换热器壳体内的氢气填充在原料油的下方，氢气对于原料油形成向上的托举力，且壳体中部介质的流速一般较为稳定，有助于原料油的分布。
并且，氢气温度升高并与原料油混合时有助于原料油部分汽化，两者在壳体内的混合效果明显优于现有技术中的底部混合进料，且不会在换热器底部形成积液。
且本申请引入高压水，高压水与热高分气换热后再与低温水进行换热，解决了现有技术中热高分气泄漏带来的安全问题，使得整个***的安全性提高。同时，引入的高压水还能用于热高分气管线的注水。
附图说明
图1为本发明实施例1的结构示意图；
图2为图1中虚线框部分的放大图；
图3为本发明实施例2的结构示意图；
图4为本发明实施例3的结构示意图；
图5为本发明实施例4的结构示意图；
图6为本发明实施例5的结构示意图；
图7为本发明实施例6的结构示意图；
图8为本发明实施例7的结构示意图；
图9为本发明实施例8的结构示意图；
图10为本发明实施例9中空冷器的结构示意图；
图11为图10中换热管与喷淋管之间的结构示意图(剖面区域为喷水区域)；
图12为图10中A-A向的剖视图；
图13为图10中集水器与中心筒之间的结构示意图；
图14为图13的俯视图；
图15为图10中的中心筒的局部结构示意图；
图16为图14中B向的结构示意图；
图17为图10中换热管的局部结构示意图；
图18为本发明实施例10中空冷器之集水器与中心筒之间的俯视图。
具体实施方式
以下结合附图实施例对本发明作进一步详细描述。
实施例1：
如图1、2所示，为本发明的一种用于加氢装置的换热组件的优选实施例1，该换热组件包括有第一换热器100、第二换热器200、第三换热器300、第五换热器500以及空冷器600。
其中，第一换热器100具有竖向设置的壳体110以及设于壳体110内并竖向延伸的螺旋换热管120，壳体110的侧壁的下部设有第一壳程入口接管111，且第一壳程入口接管111连接有用于输送氢气的氢气管线130；壳体110的侧壁的中部设有第二壳程入口接管112，且第二壳程入口接管112连接有用于输送原料油的原料油管线140；壳体110的侧壁的上部设有壳程出口接管113。同时，壳体110的顶部设有与螺旋换热管120的上端管口相连通的管程入口接管114，管程入口接管114连接有用于输送加氢装置之热高压分离罐700输出的热高分气的热高分气管线150，壳体110的底部设有与螺旋换热管120的下端管口相连通的管程出口接管115。同时，如图2所示，第一换热器100之螺旋换热管120具有竖向延伸的螺旋段120a以及位于螺旋段120a上下两侧的直管段120b；记第一换热器100之第二壳程入口接管112与螺旋段120a的下端部之间的竖直距离为H1，记螺旋段120a的上端部、下端部之间的竖直距离为H2，1/4≤H1:H2≤1/3。
本实施例中，螺旋换热管120为具有第一股换热管121和第二股换热管122的双股流换热管，管程出口接管115为一个，并同时与第一股换热管121的下端管口以及第二股换热管122的下端管口相连通。管程入口接管114有两个分别与第一股换热管121的上端管口、第二股换热管122的上端管口相连通。热高分气管线150包括有主路管线151和两个支路管线152，主路管线151的输入端用于连接至加氢装置之热高压分离罐700，主路管线151的输出端同时与两个支路管线152的输入端相连通，两个支路管线152的输出端分别与对应的管程入口接管114相连通。且每个支路管线152上均设有用于控制气体流量的第一阀门153；同时，每个支路管线152均连接有用于输送水的注水管线160，两个注水管线160上均设有用于控制流体流量的第二阀门161。沿热高分气在支路管线152内的流动方向，注水管线160与支路管线152的连通处位于上述第一阀门153的下游。
上述第五换热器500为竖向设置的单股流缠绕管式换热器，具有第五热介质通道510(为单股流缠绕管式换热器的壳程)和第五冷介质通道520(为单股流缠绕管式换热器的管程)，第五热介质通道510的输入端连接有用于输送加氢装置之加氢反应器710 输出的反应产物的产物管线530，第五热介质通道510的输出端用于连接至加氢装置之热高压分离罐700的输入端，第五冷介质通道520的输入端与第一换热器100之壳程出口接管113相连通，第五冷介质通道520的输出端用于连接至加氢反应器710的输入端。
本实施例中，第五冷介质通道520的输出端与加氢反应器710的输入端之间通过第三管线540相连通，还包括有第一旁路管线550，其两端分别与第三管线540以及原料油管线140相连通。且第一旁路管线550上设有控制流量的阀门。
同时，第三管线540上设有用于加热流体介质的加热炉560，还包括有第二旁路管线570，第二旁路管线570的输入端与上述第五换热器500之第五冷介质通道520的输出端相连通，第二旁路管线570的输出端用于连接至加氢反应器710的输入端。且第二旁路管线570以及第三管线540上均设有控制流量的阀门。
上述第二换热器200为竖向设置的单股流缠绕管式换热器，具有第二热介质通道210(为单股流缠绕管式换热器的管程)和第二冷介质通道220(为单股流缠绕管式换热器的壳程)，第二热介质通道210的输入端与上述第一换热器100之管程出口接管115之间通过第一管线240相连通(第一管线240上连接有用于供高压水的管线)，第二冷介质通道220的输入端连接有用于输送冷低分油的冷低分油管线230。
上述第三换热器300为竖向设置的单股流缠绕管式换热器，具有第三热介质通道310(为单股流缠绕管式换热器的管程)和第三冷介质通道320(为单股流缠绕管式换热器的壳程)，第三热介质通道310的输入端与上述第二换热器200之第二热介质通道210的输出端之间通过第二管线340相连通(第二管线340上连接有用于供高压水的管线)，第三冷介质通道320的输入端连接有用于输送水的供水管线330。
空冷器600为现有的高压空冷器，其入口与第三换热器300之第三热介质通道310的输出端相连通，其出口用于连接至加氢装置之冷高压分离罐720的入口。
本实施例的换热组件用于加氢装置，该加氢装置具有热高压分离罐700、加氢反应器710、冷高压分离罐720、冷低压分离罐730、热低压分离罐740。其中热高压分离罐700的顶部出口通过热高分气管线150与换热组件中第一换热器100的管程入口接管114相连通，热高压分离罐700的底部出口通过管线(管线上设有减压装置)与热低压分离罐740的入口相连通，热低压分离罐740的顶部出口通过管线(管线上设有热低分气空冷器)与冷低压分离罐730的入口相连通。冷高压分离罐720的入口与换热组件中空冷器600的出口相连通，冷高压分离罐720的底部出口通过管线(管线上设有减压装置)与冷低压分离罐730的入口相连通。冷高压分离罐720的顶部出口通过管线(管线上沿流体流向依次设有循环氢脱硫塔、压缩机缓冲罐)连接有循环泵，循环泵输出的流体分为两路，第一路走上述的氢气管线130，第二路输送至加氢反应器710。
实施例2：
如图3所示，为本发明的一种用于加氢装置的换热组件的优选实施例2，本实施例与实施例1基本相同，区别在于本实施例中第二、第三换热器组合成为一台立式换热器，且第二换热器200位于第三换热器300的上方。同时，第五换热器500、第一换热器100组合成为一台立式换热器，且第五换热器500位于第一换热器100的上方，两者之间通过管板隔开，第五换热器500之第五冷介质通道520的下端支撑于管板，并与第一换热器100之壳体110内部中空相连通。
实施例3：
如图4所示，为本发明的一种用于加氢装置的换热组件的优选实施例3，本实施例与实施例1基本相同，区别在于本实施例中第一、第二、第三换热器组合成为一台立式换热器，且第一换热器100、第二换热器200、第三换热器300依次由上至下设置。
实施例4：
如图5所示，为本发明的一种用于加氢装置的换热组件的优选实施例4，本实施例与实施例1基本相同，区别在于本实施例中第一、第二、第三、第五换热器组合成为一台立式换热器，且第五换热器500、第一换热器100、第二换热器200、第三换热器300依次由上至下设置。
实施例5：
如图6所示，为本发明的一种用于加氢装置的换热组件的优选实施例5，本实施例与实施例1基本相同，区别在于本实施例中第三换热器300上的供水管线330为用于输送高压水的管线；本实施例的换热组件还包括有第四换热器400，第四换热器400为竖向设置的单股流缠绕管式换热器，具有第四热介质通道410(为单股流缠绕管式换热器的管程)和第四冷介质通道420(为单股流缠绕管式换热器的壳程)，第四热介质通道410的输入端与第三换热器300之第三冷介质通道320的输出端相连通，第四冷介质通道420的输入端连接有用于输送低压水的低压水管线430。
同时，第四换热器400之第四热介质通道410的输出端同时与上述热高分气管线150、第一管线240以及第二管线340相连通。即本实施例中从第四热介质通道410的输出端输出的高压水可向热高分气管线150、第一管线240以及第二管线340供水，从而使得热高分气管线150、第一管线240以及第二管线340上无需再外接高压水。
并且，本实施例中第一换热器100的螺旋换热管为单股流换热管，对应地，第一换热器100的管程入口接管114只有一个，该管程入口接管114直接通过一条热高分气管线150与热高压分离罐700顶部的出口相连通。
且本实施例中，第一换热器100之第一壳程入口接管111位于螺旋段120a之下端 部的下方，壳程出口接管113位于螺旋段120a之上端部的上方。
本实施例的换热工艺如下：
一、热高压分离罐700输出的压力为9～11.5MPa、温度为230～250℃的热高分气通过管程入口接管114进入第一换热器100的螺旋换热管120内，同时，压力为10～12.5MPa、温度为70～95℃的氢气，压力为11～13.5MPa、温度为130～165℃的原料油分别从第一壳程入口接管111、第二壳程入口接管112进入壳体110内，与螺旋换热管120内的热高分气进行换热后从壳程出口接管113输出，且从壳程出口接管113输出的介质的压力为9.7～12.2MPa，温度为160～180℃，且介质中氢气的重量百分比为6～12％；
二、从第一换热器100之管程出口接管115输出的热高分气进入第二换热器200的第二热介质通道210，与第二冷介质通道220内的冷低分油进行换热，其中，进入第二冷介质通道220前的冷低分油的压力为1.0～1.8MPa，温度为48～55℃，换热后出第二冷介质通道220的冷低分油的压力为1.0～1.8MPa，温度为160～185℃；
三、从第二换热器200的第二热介质通道210输出的热高分气进入第三换热器300的第三热介质通道310，与第三冷介质通道320内的高压水进行换热，其中，进入第三冷介质通道320之前的高压水的压力为12.5～13.5MPa，温度为60～75℃；从第三热介质通道310输出的热高分气的温度为70～80℃；
四、换热后从第三冷介质通道320输出的高压水进入第四换热器400的第四热介质通道410，与第四冷介质通道420内的低压水进行换热，其中，进入第四冷介质通道420之前的低压水的压力为0.6～1.2MPa，温度为60～70℃，换热后从出第四冷介质通道420的低压水的压力为0.6～1.2MPa，温度为95～135℃；
五、从第一换热器100之壳程出口接管113输出的介质进入第五换热器500的第五冷介质通道520，与第五热介质通道510内的热介质换热后从第五换热器500输出(输出压力为9.5～12.0MPa，温度为320～365℃)，然后选择性地走第三管线540或第二旁路管线570，接着进入加氢反应器710进行加氢反应。其中，进入加氢反应器710之前的介质的压力为9.5～12.0MPa，温度为335～380℃；加氢反应器710输出的反应产物的压力为9.2～11.6MPa，温度为360～415℃，然后进入第五换热器500的第五热介质通道510内，从第五换热器500输出的反应产物进入热高压分离罐700进行气液分离。
实施例6：
如图7所示，为本发明的一种用于加氢装置的换热组件的优选实施例6，本实施例与实施例5基本相同，区别在于本实施例中第五换热器500、第一换热器100组合成为一台立式换热器，且第五换热器500位于第一换热器100的上方。且本实施例的第一换热器100的结构与实施例1中第一换热器100的结构基本相同。
实施例7：
如图8所示，为本发明的一种用于加氢装置的换热组件的优选实施例7，本实施例与实施例5基本相同，区别在于本实施例中第一、第二、第三换热器组合成为一台立式换热器，第一换热器100、第二换热器200、第三换热器300依次由上至下设置。同时本实施例的第一换热器100的结构与实施例1中第一换热器100的结构基本相同。
实施例8：
如图9所示，为本发明的一种用于加氢装置的换热组件的优选实施例8，本实施例与实施例5基本相同，区别在于本实施例中第一、第二、第三、第五换热器组合成为一台立式换热器，且第五换热器500、第一换热器100、第二换热器200、第三换热器300依次由上至下设置。
同时本实施例的第一换热器100的结构与实施例1中第一换热器100的结构基本相同，区别在于本实施例中：沿热高分气在支路管线152内的流动方向，注水管线160与支路管线152的连通处位于上述第一阀门153上游。
实施例9：
如图10～17所示，为本发明的一种用于加氢装置的换热组件的优选实施例9，本实施例与实施例1基本相同，区别在于本实施例中空冷器600的结构不同，具体如下：
本实施例的空冷器600为缠绕管式复合空冷器，其包括有壳程筒体1、两个管板、两个管箱2、中心筒3、多根换热管4、多根喷淋管5、集水箱6、水泵7、集水器8。
其中，壳程筒体1竖向设置，其下端部具有进风口11、上端部具有出风口12，且出风口12处设有风机，以使气流从进风口11进入壳程筒体1内，然后从出风口12排出。壳程筒体1的底部设有集水箱6。
两个管板分别一上一下设于壳程筒体1的侧壁上；两个管箱2分别设于各自对应的管板上，并作为空冷器600的入口和出口。
中心筒3竖向设于壳程筒体1内。且中心筒3的内部中空，其下端口31伸入上述集水箱6内。
多根换热管4沿轴向设于壳程筒体1内，且由内而外螺旋缠绕在中心筒3的外周而成多层螺旋管，相邻层螺旋管之间的间距不小于4mm，换热管4的两端分别支撑于各自对应的管板上并与对应的管箱2相连通。本实施例中，换热管4为波纹管，并具有表面光滑的光管段41和表面具有波纹的波纹段42，波纹段42与光管段41沿换热管4的长度方向交替布置，且波纹段42的长度大于光管段41的长度；具体地，波纹段42的长度为200mm，光管段41的长度为50mm。光管段41用于与固定件(如换热器用垫条) 进行配合，以固定换热管。
多根喷淋管5沿轴向设于壳程筒体1内，且沿着换热管4的螺旋方向缠绕在各层螺旋管中(各层螺旋管中有至少一根喷淋管5，这一根喷淋管5与该层的多根换热管4同步绕制，请参见图2)，各喷淋管5下端的管口为进液口51，并通过水泵7与集水箱6相连通。各喷淋管5上端的管口为开口朝下的出液口52，且出液口52位于螺旋管上方，并沿着壳程筒体1的周向等间隔布置。为了使各出液口52喷出的水流更加均匀，进一步的，各喷淋管5上端的管口连接有能向下喷水的喷头54，本实施例中，相邻3个喷头54之间以正三角形的三个端点分布，以确保每个喷头54的喷淋半径不小于150mm。各喷淋管5的管壁上还均设有多个喷淋孔53，喷淋孔53与相邻的换热管4的管壁相对，以喷淋相邻换热管。具体请参见图2，其中，多层螺旋管由内至外依次记为第一层、第二层、···、第N层，第一层中喷淋管的多个喷淋孔分别朝向第二层中换热管以及第一层中相邻布置的换热管(位于第一层中喷淋管的下方)的上表面；第N层中喷淋管的多个喷淋孔分别朝向第N-1层中换热管以及第N层中相邻布置的换热管(位于第N层中喷淋管的下方)的上表面；位于第一层、第N层之间的中间层中的喷淋管的多个喷淋孔分别朝向相邻层的换热管和同层相邻布置换热管的上表面。
上述集水器8设于壳程筒体1内并位于上述喷淋管5之出液口52的上方，且集水器8具有供气流向上通过、并能收集气流中水分的通道80。本实施例中，集水器8套设在中心筒3的外周，包括有多个竖向设置并相连的集水板81。多个集水板81之间可通过上基板或/和下基板(上下基板可以制成格栅状，也可以用带有孔的板)相连接；也可通过连接杆相连，各连接杆依次穿过各集水板81从而连接各集水板81。多个集水板81沿水平方向间隔排列，优选地，相邻两个集水板之间的间隔距离为20～50mm(间隔距离可为20mm、50mm或者两者之间的任意值)，如此设计，既能保证气水分离效果，又不影响空冷器的换热，使得相邻两个集水板81的板面之间形成上述通道80，同时，各集水板81的板面上凸设有向上延伸的唇片811，唇片811与集水板81的板面之间形成开口朝上并用于收集该唇片811之上的板面上积存水分的集水沟82，具体请参见图5、7(图5中各集水板81通过基线a来表示，基线a的数量不限于图中所示的数量，图中通过若干条基线a来表示集水板81的安装位置以及排列方向)。本实施例中，集水器8还包括有位于集水器8的中央并沿集水板81的排列方向延伸而贯穿集水板81的集水槽83，集水槽83为具有底板以及位于底板两侧的侧板的结构，底板与两个侧板之间围成截面呈U形的集水槽83。集水沟82沿集水板81的板面由外至内向集水槽83延伸并与集水槽83相连通，且集水沟82由外至内向下倾斜，以使得集水沟82内的水在自身重力作用下能流到集水槽83。上述中心筒3穿过集水槽83，中心筒3之与集水槽83相对的筒壁上设有入水口32，该入水口32与上述集水槽83相连通。如此，集水沟82内收集的水能通过集水槽83、入水口32进入中心筒3内，然后回流至集水箱6，进而实现 冷却水的重复利用。
本实施例中，为了具有更好的集水效果，上述各集水板81均自上而下制成波浪状的结构，请参见图7，各集水板81的同一侧板面上按需可以设计一个或多个集水沟82，且各集水沟82位于各集水板81的板面的外突部位处，以利于各集水板81的板面上积存的水气在下流时能完全被集水沟82所收集。
实施例10：
如图18所示，为本发明的一种用于加氢装置的换热组件的优选实施例10，本实施例与实施例9基本相同，区别在于本实施例中空冷器600之集水器8的结构略有不同，具体如下：本实施例的集水器8包括有多个竖向设置并相连接的集水板81，多个集水板81沿周向间隔排列在中心筒3的***，相邻两个集水板81的板面之间形成供气流向上通过的通道80，且各集水板81的板面上凸设有向上延伸的唇片811，唇片811与集水板81的板面之间形成开口朝上并用于收集该唇片811之上的板面积存水分的集水沟82，各集水沟82沿集水板81的板面由外至内向中心筒3延伸，且集水沟82由外至内向下倾斜。中心筒3的内部中空，且其下端口31与上述集水箱6相连通，中心筒3之与集水器8相对的筒壁上设有入水口32，该入水口32与集水沟82相连通。
如此，气流向上通过通道80时，气流中的水分会积聚在集水板81的板面上，并沿着集水板81的板面向下流到集水沟82内，集水沟82内的水在重力作用下沿着集水沟82流动至中心筒3的入水口32处，然后通过中心筒3回流至集水箱6，实现水的循环重复利用。

Claims (28)

  1. 一种用于加氢装置的换热组件，包括有第一换热器(100)，所述第一换热器(100)具有竖向设置的壳体(110)以及设于壳体(110)内并竖向延伸的螺旋换热管(120)，其特征在于：
    所述壳体(110)的侧壁的下部设有第一壳程入口接管(111)，侧壁的中部设有第二壳程入口接管(112)，侧壁的上部设有壳程出口接管(113)，且所述第一壳程入口接管(111)连接有用于输送氢气的氢气管线(130)，所述第二壳程入口接管(112)连接有用于输送原料油的原料油管线(140)；
    同时所述壳体(110)的顶部设有与螺旋换热管(120)的上端管口相连通的管程入口接管(114)，所述管程入口接管(114)连接有用于输送加氢装置之热高压分离罐(700)输出的热高分气的热高分气管线(150)，所述壳体(110)的底部设有与螺旋换热管(120)的下端管口相连通的管程出口接管(115)。
  2. 根据权利要求1所述的换热组件，其特征在于：所述螺旋换热管(120)为具有第一股换热管(121)和第二股换热管(122)的双股流换热管，所述管程入口接管(114)有两个，分别与第一股换热管(121)的上端管口、第二股换热管(122)的上端管口相连通；
    所述热高分气管线(150)包括有主路管线(151)和两个支路管线(152)，所述主路管线(151)的输入端用于连接至加氢装置之热高压分离罐(700)，所述主路管线(151)的输出端同时与两个支路管线(152)的输入端相连通，所述两个支路管线(152)的输出端分别与对应的管程入口接管(114)相连通。
  3. 根据权利要求2所述的换热组件，其特征在于：每个所述支路管线(152)上均设有用于控制气体流量的第一阀门(153)；同时，每个支路管线(152)均连接有用于输送水的注水管线(160)，两个注水管线(160)上均设有用于控制流体流量的第二阀门(161)。
  4. 根据权利要求2所述的换热组件，其特征在于：所述管程出口接管(115)为一个，并同时与上述第一股换热管(121)、第二股换热管(122)的下端管口相连通。
  5. 根据权利要求1所述的换热组件，其特征在于：所述第一换热器(100)之螺旋换热管(120)具有竖向延伸的螺旋段(120a)以及位于螺旋段(120a)上下两侧的直管段(120b)；
    记第一换热器(100)之第二壳程入口接管(112)与所述螺旋段(120a)的下端部之间的竖直距离为H1，记所述螺旋段(120a)的上端部、下端部之间的竖直距离为H2，1/4≤H1:H2≤1/3。
  6. 根据权利要求5所述的换热组件，其特征在于：所述第一换热器(100)之第一壳程入口接管(111)位于所述螺旋段(120a)之下端部的下方，所述壳程出口接管(113)位于所述螺旋段(120a)之上端部的上方。
  7. 根据权利要求1～6中任一权项所述的换热组件，其特征在于：还包括有第五换 热器(500)，具有第五热介质通道(510)和第五冷介质通道(520)，所述第五热介质通道(510)的输入端连接有用于输送加氢装置之加氢反应器(710)输出的反应产物的产物管线(530)，所述第五热介质通道(510)的输出端用于连接至加氢装置之热高压分离罐(700)的输入端，所述第五冷介质通道(520)的输入端与上述第一换热器(100)之壳程出口接管(113)相连通，所述第五冷介质通道(520)的输出端用于连接至加氢反应器(710)的输入端。
  8. 根据权利要求7所述的换热组件，其特征在于：所述第五冷介质通道(520)的输出端与加氢反应器(710)的输入端之间通过第三管线(540)相连通，还包括有第一旁路管线(550)，其两端分别与所述第三管线(540)以及原料油管线(140)相连通，且第一旁路管线(550)上设有用于控制流量的阀门。
  9. 根据权利要求8所述的换热组件，其特征在于：所述第三管线(540)上设有用于加热流体介质的加热炉(560)，还包括有第二旁路管线(570)，所述第二旁路管线(570)的输入端与上述第五冷介质通道(520)的输出端相连通，所述第二旁路管线(570)的输出端用于连接至加氢反应器(710)的输入端，且所述第二旁路管线(570)以及第三管线(540)上分别设有用于控制流量的阀门。
  10. 根据权利要求1～6中任一权项所述的换热组件，其特征在于：还包括有第二换热器(200)，具有第二热介质通道(210)和第二冷介质通道(220)，所述第二热介质通道(210)的输入端与上述第一换热器(100)之管程出口接管(115)相连通，所述第二冷介质通道(220)的输入端连接有用于输送冷低分油的冷低分油管线(230)。
  11. 根据权利要求10所述的换热组件，其特征在于：还包括有第三换热器(300)，具有第三热介质通道(310)和第三冷介质通道(320)，所述第三热介质通道(310)的输入端与上述第二换热器(200)之第二热介质通道(210)的输出端相连通，所述第三冷介质通道(320)的输入端连接有用于输送水的供水管线(330)。
  12. 根据权利要求11所述的换热组件，其特征在于：所述供水管线(330)为用于输送高压水的管线；
    还包括有第四换热器(400)，具有第四热介质通道(410)和第四冷介质通道(420)，所述第四热介质通道(410)的输入端与上述第三换热器(300)之第三冷介质通道(320)的输出端相连通，所述第四冷介质通道(420)的输入端连接有用于输送低压水的低压水管线(430)。
  13. 根据权利要求12所述的换热组件，其特征在于：所述第四换热器(400)之第四热介质通道(410)的输出端与上述热高分气管线(150)相连通；
    所述第一换热器(100)之管程出口接管(115)与所述第二换热器(200)之第二热介质通道(210)的输入端之间通过第一管线(240)相连通，该第一管线(240)与所述第四换热器(400)之第四热介质通道(410)的输出端相连通；
    所述第二换热器(200)之第二热介质通道(210)的输出端与第三换热器(300)之第三热 介质通道(310)的输入端之间通过第二管线(340)相连通，该第二管线(340)与所述第四换热器(400)之第四热介质通道(410)的输出端相连通。
  14. 根据权利要求11所述的换热组件，其特征在于：还包括有空冷器(600)，其入口与上述第三换热器(300)之第三热介质通道(310)的输出端相连通，其出口用于连接至加氢装置之冷高压分离罐(720)的入口。
  15. 根据权利要求14所述的换热组件，其特征在于：所述空冷器(600)包括有：
    壳程筒体(1)，竖向设置，其两个端部分别具有进风口(11)、出风口(12)；
    两个管板，分别一上一下设于所述壳程筒体(1)的侧壁上；
    两个管箱(2)，分别设于各自对应的管板上；
    中心筒(3)，竖向设于所述壳程筒体(1)内；
    多根换热管(4)，沿轴向设于所述壳程筒体(1)内，且由内而外螺旋缠绕在所述中心筒(3)的外周而成多层螺旋管，所述换热管(4)的两端分别支撑于各自对应的管板上并与对应的管箱(2)相连通；
    多根喷淋管(5)，沿轴向设于所述壳程筒体(1)内，且沿着换热管(4)的螺旋方向缠绕在各层螺旋管中，各喷淋管(5)下端的管口为进液口(51)，各喷淋管(5)上端的管口为开口朝下的出液口(52)，且出液口(52)位于所述螺旋管上方，并沿着壳程筒体(1)的周向间隔布置；同时，各所述喷淋管(5)的管壁上均设有多个喷淋孔(53)，所述喷淋孔(53)与相邻的换热管(4)的管壁相对。
  16. 根据权利要求15所述的换热组件，其特征在于：各喷淋管(5)上端的管口连接有能向下喷水的喷头(54)。
  17. 根据权利要求15所述的换热组件，其特征在于：所述壳程筒体(1)的底部设有集水箱(6)，所述喷淋管(5)的进液口(51)通过水泵(7)与集水箱(6)相连通。
  18. 根据权利要求17所述的换热组件，其特征在于：所述进风口(11)位于壳程筒体(1)的下端部、所述出风口(12)位于壳程筒体(1)的上端部。
  19. 根据权利要求18所述的换热组件，其特征在于：还包括有集水器(8)，设于所述壳程筒体(1)内并位于上述喷淋管(5)之出液口(52)的上方，且该集水器(8)具有供气流向上通过、并能收集气流中水分的通道(80)。
  20. 根据权利要求19所述的换热组件，其特征在于：所述集水器(8)包括有多个竖向设置并相连接的集水板(81)，多个集水板(81)沿水平方向间隔排列，相邻两个集水板(81)的板面之间形成上述通道(80)，同时，各集水板(81)的板面上凸设有向上延伸的唇片(811)，所述唇片(811)与集水板(81)的板面之间形成开口朝上并用于收集该唇片之上的板面上积存水分的集水沟(82)。
  21. 根据权利要求20所述的换热组件，其特征在于：所述集水器(8)还包括有位于集水器(8)的中央并沿集水板(81)的排列方向延伸而贯穿集水板(81)的集水槽(83)，所述集 水沟(82)沿集水板(81)的板面由外至内向集水槽(83)延伸并与集水槽(83)相连通；
    所述集水器(8)套设在上述中心筒(3)的外周，且集水槽(83)供中心筒(3)穿过，所述中心筒(3)的内部中空，且其下端口(31)与上述集水箱(6)相连通，中心筒(3)之与集水槽(83)相对的筒壁上设有与集水槽(83)相连通的入水口(32)。
  22. 根据权利要求20所述的换热组件，其特征在于：相邻两个集水板(81)之间的间隔距离为：20～50mm。
  23. 根据权利要求19所述的换热组件，其特征在于：所述集水器(8)包括有多个竖向设置并相互连接的集水板(81)，多个集水板(81)沿周向间隔排列在中心筒(3)的***，相邻两个集水板(81)的板面之间形成上述通道(80)，各集水板(81)的板面上凸设有向上延伸的唇片(811)，所述唇片(811)与集水板(81)的板面之间形成开口朝上并用于收集气流中水分的集水沟(82)，各集水沟(82)沿集水板(81)的板面由外至内向中心筒(3)延伸，所述中心筒(3)的内部中空，且其下端口(31)与上述集水箱(6)相连通，中心筒(3)之与集水器(8)相对的筒壁上设有入水口(32)，该入水口(32)与上述集水沟(82)相连通。
  24. 根据权利要求21所述的换热组件，其特征在于：所述集水沟(82)由外至内向下倾斜。
  25. 根据权利要求21所述的换热组件，其特征在于：各集水板(81)均自上而下制成波浪状的结构，各集水板(81)的同一侧板面上设有至少一个上述集水沟(82)，且各集水沟(82)位于各集水板(81)之板面的外突部位处。
  26. 根据权利要求15所述的换热组件，其特征在于：所述换热管(4)为波纹管，并具有表面光滑的光管段(41)和表面具有波纹的波纹段(42)，所述波纹段(42)与光管段(41)沿换热管(4)的长度方向交替布置，且波纹段(42)的长度大于光管段(41)的长度；
    或，所述换热管(4)为翅片管，并具有表面光滑的光管段和表面具有翅片的翅片段，所述翅片段与光管段沿换热管(4)的长度方向交替布置，且翅片段的长度大于光管段的长度。
  27. 根据权利要求15所述的换热组件，其特征在于：以上述的两个管板以及两个管箱(2)为一组，有至少两组并沿壳程筒体(1)的周向间隔布置。
  28. 一种采用如权利要求1～27中任一权项所述的换热组件的换热工艺，其特征在于步骤如下：
    热高压分离罐(700)输出的压力为9～11.5MPa、温度为230～250℃的热高分气通过管程入口接管(114)进入第一换热器(100)的螺旋换热管(120)内，同时，压力为10～12.5MPa、温度为70～95℃的氢气，压力为11～13.5MPa、温度为130～165℃的原料油分别从第一壳程入口接管(111)、第二壳程入口接管(112)进入壳体(110)内，与螺旋换热管(120)内的热高分气进行换热后从壳程出口接管(113)输出，且从壳程出口接管(113)输出的介质的压力为9.7～12.2MPa，温度为160～180℃，且介质中氢气的重量百分比为6～12％。
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