CN113063310A - Hydrogenation heat exchange system and heat exchange process adopting multi-strand wound tube type heat exchanger - Google Patents
Hydrogenation heat exchange system and heat exchange process adopting multi-strand wound tube type heat exchanger Download PDFInfo
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- CN113063310A CN113063310A CN202110478014.4A CN202110478014A CN113063310A CN 113063310 A CN113063310 A CN 113063310A CN 202110478014 A CN202110478014 A CN 202110478014A CN 113063310 A CN113063310 A CN 113063310A
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 70
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000000926 separation method Methods 0.000 claims abstract description 55
- 238000010438 heat treatment Methods 0.000 claims abstract description 37
- 239000007789 gas Substances 0.000 claims description 107
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 71
- 229910001868 water Inorganic materials 0.000 claims description 71
- 239000007795 chemical reaction product Substances 0.000 claims description 24
- 239000000203 mixture Substances 0.000 claims description 21
- 239000001257 hydrogen Substances 0.000 claims description 18
- 229910052739 hydrogen Inorganic materials 0.000 claims description 18
- 239000007788 liquid Substances 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 4
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 6
- 239000003921 oil Substances 0.000 description 37
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 13
- 239000000047 product Substances 0.000 description 8
- 239000002283 diesel fuel Substances 0.000 description 7
- 238000004804 winding Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical group N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 239000010724 circulating oil Substances 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical group [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 125000005842 heteroatom Chemical group 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 239000002184 metal Chemical group 0.000 description 1
- 229910052751 metal Chemical group 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Chemical group 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
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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
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
Abstract
A hydroprocessing heat exchange system, comprising: the device comprises a first pipeline (1), a second pipeline (2), a tenth pipeline (10), a heating furnace (6), a hydrogenation reactor (7), a heat high separation tank (8) and a heat exchange device, wherein the heat exchange device comprises a first heat exchange device (4) and a second heat exchange device (5), and the first heat exchange device (4) is connected with a heat high separation gas output end (81) of the tenth pipeline (10) and the heat high separation tank (8) for outputting heat high separation gas and is used for enabling the heat high separation gas to exchange heat with gas in the tenth pipeline (10); the second heat exchange device (5) is a second wound tube heat exchanger with one second heat medium channel (51) and at least two second cold medium channels. The application also discloses a heat exchange process for exchanging heat by adopting the hydrogenation heat exchange system. Compared with the prior art, the heat exchanger improves the heat exchange effect when the number of the heat exchangers can be reduced, and the pressure drop of the system can be reduced.
Description
Technical Field
The invention belongs to the technical field of heat exchange, and particularly relates to a hydrogenation heat exchange system and a heat exchange process adopting a multi-strand wound tubular heat exchanger.
Background
Hydrotreating is one of the important treatment methods in petroleum products, and refers to removing heteroatoms such as sulfur, nitrogen, oxygen and metal impurities in oil products under certain temperature, hydrogen partial pressure and catalyst conditions, so that olefin is saturated, and aromatic hydrocarbons are partially hydrogenated and saturated, thereby improving the service performance of the oil products.
The hydrotreating process comprises the following steps: mixing the oil product with hydrogen, feeding the mixture into a heating furnace, heating the mixture to a specified temperature, and feeding the mixture into a reactor filled with a catalyst; after the reaction is finished, hydrogen is separated in a separator and recycled by a compressor; the product is separated into hydrogen sulfide, ammonia, water and gaseous hydrogen generated by small amount decomposition in the reaction process in a stabilizing tower.
The prior heat exchange process for hydrogenation is disclosed in the invention patent application CN201310344264.4, namely a diesel oil hydrotreating process (application publication No. CN103421542A), and comprises the following steps: 1) mixing the diesel oil and the hydrogen, then carrying out heat exchange in a first heat exchanger, and heating to 280 ℃ at 270 ℃; 2) the mixture from the first heat exchanger enters a raw material heating furnace and then enters a hydrogenation reactor after being heated to 320-330 ℃; 3) the reaction product from the hydrogenation reactor is subjected to heat exchange by a fifth heat exchanger, a first heat exchanger and a second heat exchanger in sequence, then is cooled to 175-185 ℃, then is injected with water and is cooled to 45-55 ℃ by a first air cooler, and then is cooled to a high-molecular tank, and hydrogen-containing gas and cold high-molecular oil are separated; 4) hydrogen-containing gas separated from the cold high-pressure separation tank enters a circulating hydrogen compressor, is mixed with new hydrogen after being pressurized by the circulating hydrogen compressor, and is divided into two paths after being mixed, wherein one path is mixed with diesel oil, the other path enters a hydrogenation reactor, cold high-pressure separation oil discharged from the cold high-pressure separation tank is decompressed and then enters a cold low-pressure separation tank, and low-pressure separation gas and low-pressure separation oil are separated from the cold low-pressure separation tank; 5) low-fraction gas is discharged out of the cold low-fraction tank, low-fraction oil is subjected to heat exchange through a second heat exchanger, a third heat exchanger and a fifth heat exchanger in sequence and then enters a stripping fractionating tower, stripping steam is injected into the stripping fractionating tower, and then naphtha, sulfur-containing oil gas and product diesel oil are separated out from the stripping fractionating tower; 6) and respectively sending the naphtha and the sulfur-containing oil gas to the next procedure after the naphtha and the sulfur-containing oil gas come out of the stripping fractionating tower, sequentially exchanging heat of the product diesel oil by a third heat exchanger and a fourth heat exchanger, then cooling the product diesel oil by a second air cooler to 45-55 ℃, and finally entering a finished product oil tank area to obtain the diesel oil.
The equipment adopted by the hydrogenation process is high-temperature and high-pressure equipment due to harsh operating conditions, large-scale production of a conventional heat exchanger is difficult, and along with the enlargement of the scale of the equipment, the process requirements can be met only by adopting a serial/parallel connection mode of a plurality of heat exchangers in the prior art on the same number, so that the cost is undoubtedly increased, and the occupied area of the equipment is increased.
Disclosure of Invention
The first technical problem to be solved by the invention is to provide a hydrogenation heat exchange system which can reduce the number of heat exchangers and improve the heat exchange effect aiming at the current situation of the prior art.
The second technical problem to be solved by the invention is to provide a heat exchange process for heat exchange by using the hydrogenation heat exchange system, so as to improve the heat exchange effect.
The technical scheme adopted by the invention for solving the first technical problem is as follows: a hydronic heat exchange system employing a multi-stream wound tube heat exchanger, comprising: the device comprises a first pipeline for conveying raw oil, a second pipeline for conveying a bottom liquid of a stripping tower, a tenth pipeline for conveying a gas containing hydrogen, a heating furnace, a hydrogenation reactor connected with the output end of the heating furnace, a thermal high separation tank for separating a reaction product output by the hydrogenation reactor to obtain thermal high-molecular gas and thermal high-molecular oil, and a heat exchange device, and is characterized in that:
the heat exchange device comprises a first heat exchange device and a second heat exchange device, and the first heat exchange device is connected with a heat high-pressure gas output end of the tenth pipeline and the heat high-pressure separation tank, which is used for outputting heat high-pressure gas, and is used for exchanging heat between the heat high-pressure gas and the gas in the tenth pipeline;
the second heat exchange device is a second wound tube type heat exchanger with a second heat medium channel and at least two second cold medium channels, and the second wound tube type heat exchanger is provided with a second heat medium channel inlet connecting tube and a second heat medium channel outlet connecting tube which are communicated with the second heat medium channel, a second cold medium channel first inlet connecting tube and a second cold medium channel first outlet connecting tube which are communicated with the second cold medium channel first, a second cold medium channel second inlet connecting tube and a second cold medium channel second outlet connecting tube which are communicated with the second cold medium channel second; the inlet connecting pipe of the second heat medium channel is connected with the output end of the hydrogenation reactor, the outlet connecting pipe of the second heat medium channel is connected with the input end of the thermal high separation tank, the output end of the mixed pipeline after the gas output end of the first heat exchange device is connected with the first pipeline is connected with the first inlet connecting pipe of the second cold medium channel, the first outlet connecting pipe of the second cold medium channel is connected with the input end of the heating furnace, the second inlet connecting pipe of the second cold medium channel is connected with the output end of the second pipeline, and the second outlet connecting pipe of the second cold medium channel is connected to the stripping tower.
Preferably, the first heat exchange device is a first wound tube heat exchanger with one first heat medium channel and at least two first cold medium channels, the first wound tube heat exchanger is provided with a first heat medium channel inlet connecting pipe and a first heat medium channel outlet connecting pipe which are communicated with the first heat medium channel, a first cold medium channel first inlet connecting pipe and a first cold medium channel first outlet connecting pipe which are communicated with the first cold medium channel first, and a first cold medium channel second inlet connecting pipe and a first cold medium channel second outlet connecting pipe which are communicated with the first cold medium channel second;
the inlet connecting pipe of the first heat medium channel is connected with a heat high-pressure gas output end of the heat high-pressure separation tank, which is used for outputting heat high-pressure gas, the outlet connecting pipe of the first heat medium channel is connected to a second downstream device, the inlet connecting pipe of the first cold medium channel is connected with the output end of the tenth pipeline, and the outlet connecting pipe of the first cold medium channel is connected with the output end of the first pipeline; the water-cooling system also comprises a fourth pipeline for conveying water, wherein the inlet connecting pipe of the first cold medium channel is connected with the output end of the fourth pipeline, and the outlet connecting pipe of the first cold medium channel is connected to the first downstream equipment.
Also preferably, the first heat exchange device comprises a third wound tube heat exchanger with a third heat medium channel and at least one third cold medium channel, and a fourth wound tube heat exchanger with a fourth heat medium channel and at least one fourth cold medium channel, the third wound tube heat exchanger is provided with a third heat medium channel inlet connecting tube and a third heat medium channel outlet connecting tube which are communicated with the third heat medium channel, a third cold medium channel inlet connecting tube and a third cold medium channel outlet connecting tube which are communicated with the third cold medium channel, the fourth wound tube heat exchanger is provided with a fourth heat medium channel inlet connecting tube and a fourth heat medium channel outlet connecting tube which are communicated with the fourth heat medium channel, a fourth cold medium channel inlet connecting tube and a fourth cold medium channel outlet connecting tube which are communicated with the fourth cold medium channel;
the third cold medium channel inlet connecting pipe is connected with the output end of the tenth pipeline, the third cold medium channel outlet connecting pipe is connected with the first pipeline, the third hot medium channel inlet connecting pipe is connected with a hot high-pressure-distribution gas output end of the hot high-pressure separation tank, the third hot medium channel outlet connecting pipe is connected with the fourth hot medium channel inlet connecting pipe, and the fourth hot medium channel outlet connecting pipe is connected to a second downstream device; the water cooling system also comprises a fourth pipeline for conveying water, wherein the inlet connecting pipe of the fourth cold medium channel is connected with the output end of the fourth pipeline, and the outlet connecting pipe of the fourth cold medium channel is connected to the first downstream equipment.
In each of the above aspects, preferably, the second heat medium channel is a shell side of the second wound tube heat exchanger, the second cold medium channel is a tube side of the second wound tube heat exchanger, and the second heat exchange device is a double-flow wound tube heat exchanger having one shell side and two tube sides. As an alternative, the second heat medium channel may also be a tube side of the second wound tube heat exchanger, the second cold medium channel is a shell side of the second wound tube heat exchanger, and the second heat exchange device is a wound tube heat exchanger having two shell sides and one tube side.
Preferably, the first heat medium channel is a shell side of the first wound tube heat exchanger, the first cold medium channel is a tube side of the first wound tube heat exchanger, and the first heat exchange device is a double-stream wound tube heat exchanger having one shell side and two tube sides. As an alternative, the first heat medium channel may also be a tube side of the first wound tube heat exchanger, the first cold medium channel is a shell side of the first wound tube heat exchanger, and the first heat exchanging device is a wound tube heat exchanger having one tube side and two shell sides.
Preferably, the third heat medium channel is a tube side of the third wound tube heat exchanger, the third cold medium channel is a shell side of the third wound tube heat exchanger, and the third wound tube heat exchanger is a single-flow wound tube heat exchanger having one shell side and one tube side. Alternatively, the third heat medium channel may be a shell side of the third wound tube heat exchanger, and the third cold medium channel may be a tube side of the third wound tube heat exchanger.
Preferably, the fourth heat medium channel is a tube side of the fourth wound tube heat exchanger, the fourth cold medium channel is a shell side of the fourth wound tube heat exchanger, and the fourth wound tube heat exchanger is a single-flow wound tube heat exchanger having one shell side and one tube side. Alternatively, the fourth heat medium channel may be a shell side of the fourth wound tube heat exchanger, and the fourth cold medium channel may be a tube side of the fourth wound tube heat exchanger.
In each scheme, the heat recovery system further comprises a third pipeline for conveying water, and a heat high-pressure gas output end of the heat high-pressure separation tank for outputting heat high-pressure gas is connected with an output end of the third pipeline and then connected with the first heat exchange device. Therefore, water can dissolve part of media such as hydrogen sulfide and ammonium salt in the hot high-pressure gas so as to reduce the phenomenon that part of media in the hot high-pressure gas corrodes the heat exchanger. The third line may deliver water intermittently.
Preferably, the second downstream equipment is a high-pressure air cooler; the input end of the high-pressure air cooler is connected with the output end of the first heat exchange device for outputting the heat-exchanged hot high-pressure gas, and the output end of the high-pressure air cooler is connected to the cold high separation tank;
or the downstream equipment II is a wound tube heat exchanger with a hot medium channel and at least one cold medium channel, and further comprises a cold water pipeline for conveying cold water, the output end of the cold water pipeline is connected with the inlet connecting pipe of the cold medium channel of the downstream equipment II, the inlet connecting pipe of the hot medium channel of the downstream equipment II is connected with the output end of the first heat exchange device for outputting heat-exchanged hot high-pressure gas, and the outlet connecting pipe of the hot medium channel is connected to the cold high separation tank.
Namely, a wound tube type heat exchanger can be used for replacing a high-pressure air cooler, a hydrogenation device usually needs a plurality of high-pressure air coolers, and each air cooler is about 10.5 x 3m in size, large in volume and large in occupied area; and one vertically-installed winding tube type heat exchanger can meet the process requirements, so that the occupied area is greatly reduced.
Furthermore, the system also comprises a buffer tank, wherein the input end of the buffer tank is connected with the output end of the top of the cold-high separation tank, and the output end of the buffer tank is connected with the input end of the tenth pipeline. In this way, circulation of the hydrogen-containing gas can be achieved.
In the scheme, the system further comprises a cold water pipeline for conveying cold water, the number of the first cold medium channels of the first heat exchange device is at least three, and the first heat exchange device is further provided with a first cold medium channel three-inlet connecting pipe and a first cold medium channel three-outlet connecting pipe which are communicated with the first cold medium channel three; the third inlet connecting pipe of the first cold medium channel is connected with the output end of the cold water pipeline, and the third outlet connecting pipe of the first cold medium channel is connected to a third downstream device; and the second downstream equipment is a cold high separation tank. So, need not to establish high-pressure air cooler or single strand flow winding tubular heat exchanger in addition, can make the medium that comes out from first heat transfer device's hot medium passageway directly get into cold high knockout drum and separate.
In each of the above schemes, preferably, the system further includes a bypass line, a first valve and a second valve, an output end of the bypass line is connected between an output end of the heating furnace and an input end of the hydrogenation reactor, an input end of the bypass line is connected between an input end of the heating furnace and an outlet connection pipe of a second cold medium channel of the second heat exchange device, the first valve is disposed on the bypass line, and the second valve is disposed between the input end of the heating furnace and the input end of the bypass line. That is, the heating furnace in the present application is a start-up heating furnace, and only needs to perform heating operation in a start-up stage (i.e., the initial stage of system operation), and the rest stages do not need to operate. The heat exchange device can achieve better heat exchange effect, greatly reduce the operation load of the heating furnace, and can achieve the purpose by adopting the heating furnace with smaller volume and smaller heating capacity.
Preferably, the heat exchanger further comprises a fifth pipeline, a third valve and a fourth valve, wherein the input end of the fifth pipeline is connected with the mixing pipeline, and the output end of the fifth pipeline is connected with a second outlet connecting pipe of a second cold medium channel of the second heat exchanger; the third valve is arranged on the fifth pipeline, and the fourth valve is arranged between the input end of the fifth pipeline and the output end of the mixing pipeline.
The technical scheme adopted by the invention for solving the second technical problem is as follows: the heat exchange process for exchanging heat by adopting the hydrogenation heat exchange system is characterized by comprising the following steps:
inputting gas in a tenth pipeline as a cold medium into a first heat exchange device, wherein the temperature of the gas in the tenth pipeline is 60-80 ℃, the temperature of the gas discharged from the first heat exchange device is 220-250 ℃, the gas is mixed with raw oil in the first pipeline, the mixture of the gas and the raw oil and the bottom liquid of a stripping tower in a second pipeline are used as the cold medium and are input into a second heat exchange device, the temperature of the raw oil in the first pipeline is 160-210 ℃, and the temperature of the bottom liquid of the stripping tower in the second pipeline is 220-250 ℃; and (3) enabling the mixture from the second heat exchange device to enter a hydrogenation reactor for hydrogenation reaction and then output from the hydrogenation reactor, enabling the temperature of the output reaction product to be 370-440 ℃, enabling the reaction product to serve as a heat medium of the second heat exchange device to exchange heat with a cold medium in the second heat exchange device, enabling the temperature of the reaction product from the second heat exchange device to be reduced to 250 ℃, enabling the reaction product to enter a heat high separation tank to separate out heat high-component gas and heat high-component oil, enabling the separated heat high-component gas to serve as a heat medium of the first heat exchange device to exchange heat with the cold medium in the first heat exchange device, and then outputting from the first heat exchange device.
Compared with the prior art, the invention has the advantages that: the heat exchange device is designed to comprise a first heat exchange device for exchanging heat of the gas containing the hydrogen, a second heat exchange device for exchanging heat of the mixture of the gas and the raw oil after heat exchange and the bottom liquid of the stripping tower, and the second heat exchange device is a second wound tube type heat exchanger with a second heat medium channel and at least two second cold medium channels, so that the number of the heat exchangers can be reduced, and further the occupied area of equipment, the investment of a frame, the using amount of high-pressure pipelines, the work of pipe distribution, the maintenance cost of the equipment and the like are reduced; in addition, the first heat exchange device and the second heat exchange device can be matched to realize and improve the heat exchange effect after the combination of a plurality of heat exchangers in the prior art, hydrogenation reaction can be carried out without a heating furnace after the operation is stable, and the temperature difference of the hot end and the pressure drop of a medium are small; the bypass adjusting means of the heat exchange device is consistent with that of the prior art; meanwhile, the pressure drop of the whole device can be reduced, and the advantages are obvious; and the structure is simple and convenient to implement.
Drawings
FIG. 1 is a schematic structural diagram according to a first embodiment of the present invention;
FIG. 2 is a schematic structural diagram according to a second embodiment of the present invention;
FIG. 3 is a schematic structural diagram of a third embodiment of the present invention;
FIG. 4 is a schematic structural diagram of a fourth embodiment of the present invention;
fig. 5 is a schematic structural diagram of a first heat exchange device in a fifth embodiment of the present invention;
fig. 6 is a schematic structural diagram of a first heat exchange device in a sixth embodiment of the present invention.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
The first embodiment is as follows:
as shown in fig. 1, a first preferred embodiment of a hydrogenation heat exchange system and a heat exchange process using a multi-stream wound tube heat exchanger according to the present invention includes a first pipeline 1, a second pipeline 2, a third pipeline 3, a fourth pipeline 30, a tenth pipeline 10, a cold water pipeline 100, a fifth pipeline 150, a third valve 150, a fourth valve 160, a bypass pipeline 110, a first valve 120, a second valve 130, a first heat exchange device 4, a second heat exchange device 5, a heating furnace 6, a hydrogenation reactor 7, and a hot high separation tank 8.
Wherein, the first pipeline 1 is used for conveying raw oil; and a first buffer tank 95 and a circulating oil line for transporting circulating oil are connected to the first pipeline 1. The second line 2 is used to convey the stripper bottoms. The third line 3 is used for transporting water. The fourth line 30 is for transporting water. The tenth line is for transporting a hydrogen-containing gas. Cold water line 100 is used to deliver cold water.
The input end of the hydrogenation reactor 7 is connected with the output end of the heating furnace 6, the thermal high-pressure separation tank 8 is used for separating a reaction product output by the hydrogenation reactor 7 to obtain thermal high-pressure gas and thermal high-pressure oil, the thermal high-pressure separation tank 8 is provided with a thermal high-pressure gas output end 81 for outputting the thermal high-pressure gas and a thermal high-pressure oil output end 82 for outputting the thermal high-pressure oil, and the thermal high-pressure oil output end 82 is connected with a downstream device.
The first heat exchange device 4 is a first wound tube heat exchanger having one first heat medium channel 41 and two first cold medium channels, and the first wound tube heat exchanger is provided with a first heat medium channel inlet connecting pipe 411 and a first heat medium channel outlet connecting pipe 412 which are communicated with the first heat medium channel 41, a first cold medium channel first inlet connecting pipe 421 and a first cold medium channel first outlet connecting pipe 422 which are communicated with the first cold medium channel first 42, and a first cold medium channel second inlet connecting pipe 431 and a first cold medium channel second outlet connecting pipe 432 which are communicated with the first cold medium channel second 43; in this embodiment, the first heat medium channel 41 is a shell side of the first wound tube heat exchanger, the first cold medium channel is a tube side of the first wound tube heat exchanger, and the first heat exchanging device 4 is a double-flow wound tube heat exchanger having one shell side and two tube sides.
The second heat exchange device 5 is a second wound tube heat exchanger having one second heat medium channel 51 and two second cold medium channels, and the second wound tube heat exchanger is provided with a second heat medium channel inlet connecting pipe 511 and a second heat medium channel outlet connecting pipe 512 which are communicated with the second heat medium channel 51, a second cold medium channel first inlet connecting pipe 521 and a second cold medium channel first outlet connecting pipe 522 which are communicated with the second cold medium channel first 52, and a second cold medium channel second inlet connecting pipe 531 and a second cold medium channel second outlet connecting pipe 532 which are communicated with the second cold medium channel second 53; the second heat medium channel 51 and the second cold medium channel are the tube side and the shell side of the second wound tube heat exchanger; in this embodiment, the second heat medium channel 51 is a shell pass of the second wound tube heat exchanger, the second cold medium channel is a tube pass of the second wound tube heat exchanger, and the second heat exchanging device 5 is a double-flow wound tube heat exchanger having one shell pass and two tube passes.
The connection structure between the first heat exchange device 4 and the second heat exchange device 5 and the pipelines, the heating furnace 6, the hydrogenation reactor 7 and the thermal high separation tank 8 is as follows: the hot high branch gas output end 81 is connected with the output end of the third pipeline 3 and then connected with the first heat medium channel inlet connecting pipe 411 in the first heat exchanging device 4, the first heat medium channel outlet connecting pipe 412 is connected with the second downstream equipment 9, the first cold medium channel first inlet connecting pipe 421 is connected with the output end of the tenth pipeline 10, the output end of the mixed pipeline after the first cold medium channel first outlet connecting pipe 422 is connected with the first pipeline 1 is connected with the second cold medium channel first inlet connecting pipe 521 in the second heat exchanging device 5, the first cold medium channel second inlet connecting pipe 431 is connected with the output end of the fourth pipeline 30, and the first cold medium channel second outlet connecting pipe 432 is connected with the first downstream equipment. In the second heat exchanger 5, a second heat medium channel inlet connection pipe 511 is connected to the output end of the hydrogenation reactor 7, a second heat medium channel outlet connection pipe 512 is connected to the input end of the thermal high separation tank 8, a second cold medium channel first outlet connection pipe 522 is connected to the input end of the heating furnace 6, a second cold medium channel second inlet connection pipe 531 is connected to the output end of the second pipeline 2, and a second cold medium channel second outlet connection pipe 532 is connected to the stripping column.
In this embodiment, the second downstream equipment 9 is a high-pressure air cooler, and the heat medium from the first heat medium channel outlet connection pipe 412 passes through the high-pressure air cooler and then is connected to the cold high separation tank 93 to separate the gas containing hydrogen. The system further comprises a buffer tank 94, the input end of the buffer tank 94 is connected with the output end of the top of the cold-high separation tank 93, and the output end of the top of the buffer tank 94 is connected with the input end of the tenth pipeline 10, so that the cyclic utilization of gas is realized. Of course, a hydrogen line for replenishing hydrogen may be connected to the tenth line 10. And a pipeline for continuously conveying water can be connected between the first heat medium channel outlet connecting pipe 412 and the input end of the second downstream device 9.
The output end of the bypass pipeline 110 is connected between the output end of the heating furnace 6 and the input end of the hydrogenation reactor 7, the input end of the bypass pipeline 110 is connected between the input end of the heating furnace 6 and an outlet connecting pipe 522 of the second cold medium channel of the second heat exchange device 5, the first valve 120 is arranged on the bypass pipeline 110, and the second valve 130 is arranged between the input end of the heating furnace 6 and the input end of the bypass pipeline 110. The input end of the fifth pipeline 140 is connected to the mixing pipeline, and the output end is connected to an outlet connection pipe 522 of the second refrigerant channel of the second heat exchange device 5; a third valve 150 is provided on the fifth line 140 and a fourth valve 160 is provided between the input of the fifth line 140 and the output of the mixing line. The bypass line 110, the fifth line 140 and the valves are arranged to meet the process conditions of the device in various stages and various working conditions. The on-off of each pipeline is selected according to the actual working condition.
The method for exchanging heat by adopting the hydrogenation heat exchange system of the embodiment comprises the following steps:
respectively inputting gas in a tenth pipeline 10 and water in a fourth pipeline 30 serving as cold media into corresponding tube passes of the first heat exchange device 4, wherein the temperature of the gas in the tenth pipeline 10 is 60-80 ℃, and the temperature of the water in the fourth pipeline 30 is 60-75 ℃; the temperature of the gas and the water discharged from the first heat exchange device 4 is 220-250 ℃ and 95-125 ℃ respectively. Mixing gas from a first heat exchange device 4 with raw oil in a first pipeline 1, respectively inputting a mixture formed by the gas and the raw oil and stripper base liquid in a second pipeline 2 serving as cold media into corresponding tube passes in a second heat exchange device 5, wherein the temperature of the raw oil in the first pipeline 1 is 160-210 ℃, and the temperature of the stripper base liquid in the second pipeline 2 is 220-250 ℃; the temperature of the mixture from the tube pass of the second heat exchange device 5 and the temperature of the bottom liquid of the stripping tower are 350-395 ℃ and 270-290 ℃ respectively, the mixture from the tube pass of the second heat exchange device 5 enters the hydrogenation reactor 7 for hydrogenation reaction and then is output from the hydrogenation reactor 7, the temperature of the output reaction product is 370-440 ℃, the reaction product is taken as the heat medium of the second heat exchange device 5 to go out of the shell pass of the second heat exchange device 5 for heat exchange with the cold medium in the second heat exchange device 5, the temperature of the reaction product from the shell pass of the second heat exchange device 5 is reduced to 250 ℃, the reaction product enters the heat high separation tank 8 for separating heat high-fraction gas and heat high-fraction oil, the separated heat high-fraction gas is mixed with the water in the third pipeline 3 and then taken as the heat medium of the first heat exchange device 4 to go out of the shell pass of the first heat exchange device 4 for heat exchange with the cold medium in the tube pass of the first heat exchange device 4, and then the hot high-pressure gas and the water are output from the first heat exchange device 4, the temperature of the hot high-pressure gas and the water from the shell pass of the first heat exchange device 4 is reduced to 80-105 ℃, the hot high-pressure gas and the water enter the second downstream equipment 9, the temperature of the medium from the second downstream equipment 9 is 50 ℃, the hot high-pressure gas and the water enter the cold high-pressure separation tank 93 for separation, the gas from the top of the cold high-pressure separation tank 93 enters the buffer tank 94, and the gas from the top of the buffer tank 94 enters the tenth pipeline 10 to realize the circulation of the gas. The content ratio between the gas in the mixing pipeline and the raw oil in the embodiment is designed according to actual working conditions.
The hydrogenation heat exchange system of the embodiment has high heat exchange efficiency, so that the mixture coming out of the second heat exchange device 5 can directly enter the hydrogenation reactor 7 for reaction without being heated by the heating furnace, the heating furnace is only used at the initial stage of operation, and the bypass pipeline 110 can be used at other operation stages.
Example two:
as shown in fig. 2, in a second preferred embodiment of a hydrogenation heat exchange system and a heat exchange process using a multi-stream wound tube heat exchanger according to the present invention, this embodiment is substantially the same as the first embodiment, except that the first heat exchange device 4 in this embodiment is different from the first embodiment, the first heat exchange device 4 in this embodiment includes a third wound tube heat exchanger 4a having a third heat medium channel 45 and a third cold medium channel 46, and a fourth wound tube heat exchanger 4b having a fourth heat medium channel 47 and a fourth cold medium channel 48, the third wound tube heat exchanger 4a is provided with a third heat medium channel inlet connection pipe 451 and a third heat medium channel outlet connection pipe 452 communicating with the third heat medium channel 45, and a third cold medium channel inlet connection pipe 461 and a third cold medium channel outlet 462 communicating with the third cold medium channel 46, the fourth wound tube heat exchanger 4b is provided with a fourth heat medium channel inlet connection 471 and a fourth heat medium channel outlet connection 472 which are communicated with the fourth heat medium channel 47, and a fourth cold medium channel inlet connection 481 and a fourth cold medium channel outlet connection 482 which are communicated with the fourth cold medium channel 48. In this embodiment, the third heat medium channel 45 is a tube side of the third wound tube heat exchanger 4a, the third cooling medium channel 46 is a shell side of the third wound tube heat exchanger 4a, and the third wound tube heat exchanger 4a is a single-flow wound tube heat exchanger having one shell side and one tube side. The fourth heat medium passage 47 is the tube side of the fourth wound tube heat exchanger 4b, the fourth cold medium passage 48 is the shell side of the fourth wound tube heat exchanger 4b, and the fourth wound tube heat exchanger 4b is a single-flow wound tube heat exchanger having one shell side and one tube side.
The connection structure between the first heat exchange device 4 and each pipeline, the second heat exchange device 5 and the hot high-pressure gas distribution output end 81 in the embodiment is as follows: a third cold medium channel inlet connecting pipe 461 in the third winding pipe type heat exchanger 4a is connected with the output end of the tenth pipeline 10, the output end of the mixing pipeline after the third cold medium channel outlet connecting pipe 462 is connected with the first pipeline 1 is connected with a first cold medium channel inlet connecting pipe 521 in the second heat exchanging device 5, a hot high-pressure gas output end 81 is connected with the output end of the third pipeline 3 and then is connected with a third hot medium channel inlet connecting pipe 451, a third hot medium channel outlet connecting pipe 452 is connected with a fourth hot medium channel inlet connecting pipe 471 in the fourth winding pipe type heat exchanger 4b, the fourth hot medium channel outlet connecting pipe 472 is connected with a second downstream device 9, the fourth cold medium channel inlet connecting pipe 481 is connected with the output end of the fourth pipeline 30, and the fourth cold medium channel outlet connecting pipe 482 is connected with a first downstream device.
In this embodiment, a line for continuously supplying water or intermittently supplying water is connected between the third thermal medium passage outlet connection pipe 452 and the fourth thermal medium passage inlet connection pipe 471.
The method for exchanging heat by adopting the hydrogenation heat exchange system of the embodiment comprises the following steps:
inputting the gas in the tenth pipeline 10 as a cold medium into the shell side of the third wound tube type heat exchanger 4a, wherein the temperature of the gas in the tenth pipeline 10 is 60-80 ℃, and the temperature of the gas coming out of the shell side of the third wound tube type heat exchanger 4a is 220-250 ℃; and (3) inputting water in a fourth pipeline 30 as a cold medium into the shell side of the fourth wound tubular heat exchanger 4b, wherein the temperature of the water in the fourth pipeline 30 is 60-75 ℃, and the temperature of the water discharged from the shell side of the fourth wound tubular heat exchanger 4b is 95-125 ℃. Mixing gas discharged from the shell side of the third wound tube type heat exchanger 4a with raw oil in the first pipeline 1, respectively inputting a mixture consisting of the gas and the raw oil and a bottom liquid of a stripping tower in the second pipeline 2 into respective corresponding tube sides of the second heat exchange device 5 as cold media, wherein the temperature of the raw oil in the first pipeline 1 is 160-210 ℃, and the temperature of the bottom liquid of the stripping tower in the second pipeline 2 is 220-250 ℃; the temperature of the mixture from the tube pass of the second heat exchange device 5 and the temperature of the bottom liquid of the stripping tower are 350-395 ℃ and 270-290 ℃ respectively, the mixture from the tube pass of the second heat exchange device 5 enters the hydrogenation reactor 7 for hydrogenation reaction and then is output from the hydrogenation reactor 7, the temperature of the output reaction product is 370-440 ℃, the reaction product is taken as a heat medium of the second heat exchange device 5 to go through the shell pass of the second heat exchange device 5 for heat exchange with a cold medium in the second heat exchange device 5, the temperature of the reaction product from the shell pass of the second heat exchange device 5 is reduced to 250 ℃, the reaction product enters the thermal high-temperature separation tank 8 for separating thermal high-temperature component gas and thermal high-temperature component oil, the separated thermal high-temperature component gas is mixed with water in the third pipeline 3 and then taken as a heat medium to sequentially go through the tube pass of the third winding tube type heat exchanger 4a and the tube pass of the fourth winding tube type heat exchanger 4b, and the third winding tube type heat exchanger 4a, The cold medium in the shell pass of the fourth wound tube type heat exchanger 4b exchanges heat, then the cold medium is output from the tube pass of the fourth wound tube type heat exchanger 4b, the temperature of hot high-pressure gas and water discharged from the tube pass of the fourth wound tube type heat exchanger 4b is reduced to 80-105 ℃, the hot high-pressure gas and the water enter the second downstream equipment 9, the temperature of the medium discharged from the second downstream equipment 9 is 50 ℃, the medium enters the cold high-pressure separation tank 93 for separation, the gas discharged from the top of the cold high-pressure separation tank 93 enters the buffer tank 94, and the gas discharged from the top of the buffer tank 94 enters the tenth pipeline 10, so that the circulation of the gas is realized.
The hydrogenation heat exchange system of the embodiment has high heat exchange efficiency, so that the mixture coming out of the second heat exchange device 5 can directly enter the hydrogenation reactor 7 for reaction without being heated by the heating furnace, the heating furnace is only used at the initial stage of operation, and the bypass pipeline 110 can be used at other operation stages.
Example three:
as shown in fig. 3, a third preferred embodiment of a hydrogenation heat exchange system and a heat exchange process using a multi-stream wound tube heat exchanger according to the present invention is substantially the same as the second preferred embodiment, except that the second downstream equipment 9 in this embodiment is a wound tube heat exchanger having one hot medium channel 92 and one cold medium channel 91, and this embodiment further includes a cold water pipeline 100 for transporting cold water, an output end of the cold water pipeline 100 is connected to an inlet connection pipe of the cold medium channel 91 of the second downstream equipment 9, an outlet connection pipe of the cold medium channel 91 is connected to the third downstream equipment, an inlet connection pipe of the hot medium channel 92 of the second downstream equipment 9 is connected to an output end of the first heat exchange device 4 for outputting heat-exchanged hot high-split gas (in this embodiment, an output end of the first heat exchange device 4 for outputting heat-exchanged hot high-split gas is a fourth hot medium channel outlet connection pipe 472), the outlet connection of the heat medium channel 92 is connected to a cold high separation tank 93. And a line for continuously supplying water or intermittently supplying water is connected between the fourth heat medium passageway outlet connection pipe 472 and the inlet connection pipe of the heat medium passageway 92 of the second downstream device 9.
The heat exchange method of this embodiment is substantially the same as that of the second embodiment, except that the temperature of the cold water in the cold water line 100 in this embodiment is less than 35 ℃, the temperature of the cold water output from the cold medium channel 91 of the second downstream device 9 is less than 45 ℃, the temperature of the medium before entering the hot medium channel 92 of the second downstream device 9 is 80-105 ℃, and the temperature of the medium output from the hot medium channel 92 of the second downstream device 9 is 50 ℃.
Example four:
as shown in fig. 4, a fourth preferred embodiment of a hydrogenation heat exchange system and a heat exchange process using a multi-stream wound tube heat exchanger according to the present invention is basically the same as the first embodiment, except that the first heat exchange device 4 in the present embodiment is slightly different from the first heat exchange device in the first embodiment, the first heat exchange device 4 in the present embodiment has one first heat medium channel 41 and three first cold medium channels, the three first cold medium channels are a first cold medium channel one 42, a first cold medium channel two 43 and a first cold medium channel three 44, respectively, and the first heat exchange device 4 is further provided with a first cold medium channel three-inlet 441 and a first cold medium channel three-outlet connection pipe 442 which are communicated with the first cold medium channel three 44. Meanwhile, the present embodiment further includes a cold water pipeline 100 for delivering cold water, the first three-inlet connection pipe 441 of the cold medium channel is connected to the output end of the cold water pipeline 100, and the first three-outlet connection pipe 442 of the cold medium channel is connected to the third downstream device. As such, the water in the cold water line 100 may be heated, and the downstream device three may be a device that requires water for use or a line that delivers water. And the outlet connection pipe 412 of the first heat medium channel is directly connected to the cold-high separation tank 93 in this embodiment without additionally providing the second downstream equipment 9.
The method for exchanging heat by adopting the hydrogenation heat exchange system of the embodiment comprises the following steps:
respectively inputting gas in a tenth pipeline 10, water in a fourth pipeline 30 and cold water in a cold water pipeline 100 as cold media into corresponding tube passes of the first heat exchange device 4, wherein the temperature of the gas in the tenth pipeline 10 is 60-80 ℃, the temperature of the water in the fourth pipeline 30 is 60-75 ℃, and the temperature of the cold water in the cold water pipeline 100 is less than 35 ℃; the temperature of the gas, the water and the cold water discharged from the tube pass of the first heat exchange device 4 is 220-250 ℃, 95-125 ℃ and less than 45 ℃. Mixing gas discharged from a tube pass of a first heat exchange device 4 with raw oil in a first pipeline 1, taking a mixture formed by the gas and the raw oil and a bottom liquid of a stripping tower in a second pipeline 2 as cold media to be respectively input into the corresponding tube passes of a second heat exchange device 5, wherein the temperature of the raw oil in the first pipeline 1 is 160-210 ℃, and the temperature of the bottom liquid of the stripping tower in the second pipeline 2 is 220-250 ℃; the temperature of the mixture from the tube pass of the second heat exchange device 5 and the temperature of the bottom liquid of the stripping tower are 350-395 ℃ and 270-290 ℃ respectively, the mixture from the tube pass of the second heat exchange device 5 enters the hydrogenation reactor 7 for hydrogenation reaction and then is output from the hydrogenation reactor 7, the temperature of the output reaction product is 370-440 ℃, the reaction product is taken as the heat medium of the second heat exchange device 5 to go out of the shell pass of the second heat exchange device 5 for heat exchange with the cold medium in the second heat exchange device 5, the temperature of the reaction product from the shell pass of the second heat exchange device 5 is reduced to 250 ℃, the reaction product enters the heat high separation tank 8 for separating heat high-fraction gas and heat high-fraction oil, the separated heat high-fraction gas is mixed with the water in the third pipeline 3 and then taken as the heat medium of the first heat exchange device 4 to go out of the shell pass of the first heat exchange device 4 for heat exchange with the cold medium in the tube pass of the first heat exchange device 4, then, the temperature of the hot high-pressure gas and the water discharged from the shell pass of the first heat exchange device 4 is reduced to 50 ℃ from the first heat exchange device 4, and then the hot high-pressure gas and the water enter a cold high separation tank 93 for separation, the gas discharged from the top of the cold high separation tank 93 enters a buffer tank 94, and the gas discharged from the top of the buffer tank 94 enters a tenth pipeline 10, so that the circulation of the gas is realized.
The hydrogenation heat exchange system of the embodiment has high heat exchange efficiency, so that the mixture coming out of the second heat exchange device 5 can directly enter the hydrogenation reactor 7 for reaction without being heated by the heating furnace, the heating furnace is only used at the initial stage of operation, and the bypass pipeline 110 can be used at other operation stages.
Example five:
as shown in fig. 5, a fifth preferred embodiment of a hydrogenation heat exchange system and a heat exchange process using a multi-stream wound tube heat exchanger according to the present invention is basically the same as the first embodiment, except that the first heat exchange device in the present embodiment is slightly different from the first heat exchange device in the first embodiment, in the present embodiment, the first heat medium channel 41 is a tube side of the first heat exchange device 4, the first cold medium channel is a shell side of the first heat exchange device 4, and the first heat exchange device 4 is a wound tube heat exchanger having two shell sides and one tube side.
The second heat exchange device in this embodiment may refer to the structural design of the first heat exchange device in this embodiment, and may also be set up with the structure of the first heat exchange device in the first embodiment, specifically selected according to actual conditions.
Example six:
as shown in fig. 6, a sixth preferred embodiment of a hydrogenation heat exchange system and a heat exchange process using a multi-stream wound tube heat exchanger according to the present invention is basically the same as the fourth embodiment, except that the first heat exchange device in the present embodiment is slightly different from the first heat exchange device in the fourth embodiment, the first heat medium channel 41 in the present embodiment is a tube side of the first heat exchange device 4, the first cold medium channel is a shell side of the first heat exchange device 4, and the first heat exchange device 4 is a wound tube heat exchanger having three shell sides and one tube side.
The temperatures of raw oil, gas, bottom liquid of the stripping tower and the like in the embodiments can adopt different temperatures according to actual working conditions, the data are shown, and only after the heat exchange device in the embodiments is adopted, the heat exchange effect is good compared with the heat exchange device in the existing hydrogenation process, so that the number of heat exchangers can be reduced, the occupied area of equipment, the equipment investment, the using amount of high-pressure pipelines, the piping work, the maintenance cost of the equipment and the like can be reduced, the pressure drop of the whole device can also be reduced, the whole structure is simple, and the implementation is convenient.
Claims (13)
1. A hydronic heat exchange system employing a multi-stream wound tube heat exchanger, comprising: a high knockout drum (8) and heat transfer device for carrying first pipeline (1) of raw oil, a second pipeline (2) for carrying the stripper bottom liquor, a tenth pipeline (10) for carrying the gas that contains hydrogen, heating furnace (6), hydrogenation ware (7) that links to each other with the output of heating furnace (6), a reaction product that is used for exporting hydrogenation ware (7) separates in order to obtain high branch gas of heat and high branch oil of heat, its characterized in that:
the heat exchange device comprises a first heat exchange device (4) and a second heat exchange device (5), the first heat exchange device (4) is connected with the tenth pipeline (10) and a hot high-pressure gas output end (81) of the hot high-pressure separation tank (8) for outputting hot high-pressure gas, and the first heat exchange device is used for enabling the hot high-pressure gas to exchange heat with the gas in the tenth pipeline (10);
the second heat exchange device (5) is a second wound tube type heat exchanger with a second heat medium channel (51) and at least two second cold medium channels, and the second wound tube type heat exchanger is provided with a second heat medium channel inlet connecting pipe (511) and a second heat medium channel outlet connecting pipe (512) which are communicated with the second heat medium channel (51), a second cold medium channel first inlet connecting pipe (521) and a second cold medium channel first outlet connecting pipe (522) which are communicated with a second cold medium channel first (52), a second cold medium channel second inlet connecting pipe (531) and a second cold medium channel second outlet connecting pipe (532) which are communicated with a second cold medium channel second (53); the second heat medium channel inlet connecting pipe (511) is connected with the output end of the hydrogenation reactor (7), the second heat medium channel outlet connecting pipe (512) is connected with the input end of the high-temperature separation tank (8), the output end of a mixed pipeline after the gas output end of the first heat exchange device (4) is connected with the first pipeline (1) is connected with the second cold medium channel first inlet connecting pipe (521), the second cold medium channel first outlet connecting pipe (522) is connected with the input end of the heating furnace (6), the second cold medium channel second inlet connecting pipe (531) is connected with the output end of the second pipeline (2), and the second cold medium channel second outlet connecting pipe (532) is connected to the stripping tower.
2. The hydrogenation heat exchange system of claim 1, wherein: the first heat exchange device (4) is a first wound tube type heat exchanger with a first heat medium channel (41) and at least two first cold medium channels, and the first wound tube type heat exchanger is provided with a first heat medium channel inlet connecting pipe (411) and a first heat medium channel outlet connecting pipe (412) which are communicated with the first heat medium channel (41), a first cold medium channel first inlet connecting pipe (421) and a first cold medium channel first outlet connecting pipe (422) which are communicated with the first cold medium channel I (42), a first cold medium channel second inlet connecting pipe (431) and a first cold medium channel second outlet connecting pipe (432) which are communicated with the first cold medium channel II (43);
the first heat medium channel inlet connecting pipe (411) is connected with a heat high-pressure gas output end (81) of the heat high-pressure separation tank (8) for outputting heat high-pressure gas, the first heat medium channel outlet connecting pipe (412) is connected to a second downstream device (9), the first cold medium channel inlet connecting pipe (421) is connected with the output end of the tenth pipeline (10), and the first cold medium channel outlet connecting pipe (422) is connected with the output end of the first pipeline (1); the water-cooling system also comprises a fourth pipeline (30) for conveying water, wherein the inlet connecting pipe (431) of the first cold medium channel is connected with the output end of the fourth pipeline (30), and the outlet connecting pipe (432) of the first cold medium channel is connected to the first downstream equipment.
3. The hydrogenation heat exchange system of claim 1, wherein: the first heat exchange device (4) comprises a third wound tube type heat exchanger (4a) with a third heat medium channel (45) and at least one third cold medium channel (46), and a fourth wound tube type heat exchanger (4b) with a fourth heat medium channel (47) and at least one fourth cold medium channel (48), wherein a third heat medium channel inlet connecting pipe (451) and a third heat medium channel outlet connecting pipe (452) which are communicated with the third heat medium channel (45) are arranged on the third wound tube type heat exchanger (4a), a third cold medium channel inlet connecting pipe (461) and a third cold medium channel outlet connecting pipe (462) which are communicated with the third cold medium channel (46) are arranged on the fourth wound tube type heat exchanger (4b), and a fourth heat medium channel inlet connecting pipe (471) and a fourth heat medium channel outlet connecting pipe (472) which are communicated with the fourth heat medium channel (47) are arranged on the fourth wound tube type heat exchanger (4b), A fourth cold medium channel inlet connection pipe (481) and a fourth cold medium channel outlet connection pipe (482) which are communicated with the fourth cold medium channel (48);
the third cold medium channel inlet connecting pipe (461) is connected with the output end of the tenth pipeline (10), the third cold medium channel outlet connecting pipe (462) is connected with the first pipeline (1), the third heat medium channel inlet connecting pipe (451) is connected with a heat high-pressure gas output end (81) of the heat high-pressure separation tank (8) for outputting heat high-pressure gas, the third heat medium channel outlet connecting pipe (452) is connected with the fourth heat medium channel inlet connecting pipe (471), and the fourth heat medium channel outlet connecting pipe (472) is connected with a second downstream device (9); and the cold medium pipeline further comprises a fourth pipeline (30) for conveying water, the fourth cold medium channel inlet connecting pipe (481) is connected with the output end of the fourth pipeline (30), and the fourth cold medium channel outlet connecting pipe (482) is connected to the first downstream equipment.
4. The hydrogenation heat exchange system according to any one of claims 1 to 3, wherein: the second heat medium channel (51) is a shell pass of the second wound tube heat exchanger, the second cold medium channel is a tube pass of the second wound tube heat exchanger, and the second heat exchange device (5) is a double-flow wound tube heat exchanger with one shell pass and two tube passes.
5. The hydrogenation heat exchange system of claim 2, wherein: the first heat medium channel (41) is a shell pass of the first wound tube heat exchanger, the first cold medium channel is a tube pass of the first wound tube heat exchanger, and the first heat exchange device (4) is a double-flow wound tube heat exchanger with one shell pass and two tube passes.
6. The hydrogenation heat exchange system of claim 3, wherein: the third heat medium channel (45) is the tube side of the third wound tube heat exchanger (4a), the third cold medium channel (46) is the shell side of the third wound tube heat exchanger (4a), and the third wound tube heat exchanger (4a) is a single-flow wound tube heat exchanger having one shell side and one tube side;
the fourth heat medium channel (47) is a tube side of the fourth wound tube heat exchanger (4b), the fourth cold medium channel (48) is a shell side of the fourth wound tube heat exchanger (4b), and the fourth wound tube heat exchanger (4b) is a single-flow wound tube heat exchanger having one shell side and one tube side.
7. The hydrogenation heat exchange system according to any one of claims 1 to 3, wherein: the heat exchange system is characterized by further comprising a third pipeline (3) used for conveying water, wherein a heat high-pressure gas output end (81) of the heat high-pressure separation tank (8) used for outputting heat high-pressure gas is connected with the output end of the third pipeline (3) and then connected with the first heat exchange device (4).
8. The hydroprocessing heat exchange system of claim 2 or 3, wherein: the second downstream equipment (9) is a high-pressure air cooler, the input end of the high-pressure air cooler is connected with the output end of the first heat exchange device (4) for outputting the heat-exchanged hot high-pressure gas, and the output end of the high-pressure air cooler is connected to the cold high separation tank (93);
or the downstream equipment II (9) is a wound tube type heat exchanger with a heat medium channel (92) and at least one cold medium channel (91), and further comprises a cold water pipeline (100) for conveying cold water, the output end of the cold water pipeline (100) is connected with the inlet connecting pipe of the cold medium channel (91) of the downstream equipment II (9), the inlet connecting pipe of the heat medium channel (92) of the downstream equipment II (9) is connected with the output end of the first heat exchange device (4) for outputting heat-exchanged high-pressure gas, and the outlet connecting pipe of the heat medium channel (92) is connected to the cold high separation tank (93).
9. The hydroprocessing heat exchange system of claim 8, wherein: the cold-high separation device is characterized by further comprising a buffer tank (94), wherein the input end of the buffer tank (94) is connected with the output end of the top of the cold-high separation tank (93), and the output end of the buffer tank (94) is connected with the input end of the tenth pipeline (10).
10. The hydrogenation heat exchange system of claim 2, wherein: the heat exchanger also comprises a cold water pipeline (100) for conveying cold water, at least three first cold medium channels of the first heat exchanger (4) are provided, and the first heat exchanger (4) is also provided with a first cold medium channel three-inlet connecting pipe (441) and a first cold medium channel three-outlet connecting pipe (442) which are communicated with the first cold medium channel three (44); the first cold medium channel three-inlet connecting pipe (441) is connected with the output end of the cold water pipeline (100), and the first cold medium channel three-outlet connecting pipe (442) is connected to a downstream device three; and the second downstream equipment (9) is a cold high separation tank (93).
11. The hydrogenation heat exchange system according to any one of claims 1 to 3, wherein: the heat exchanger is characterized by further comprising a bypass pipeline (110), a first valve (120) and a second valve (130), wherein the output end of the bypass pipeline (110) is connected between the output end of the heating furnace (6) and the input end of the hydrogenation reactor (7), the input end of the bypass pipeline (110) is connected between the input end of the heating furnace (6) and an outlet connecting pipe (522) of a second cold medium channel of the second heat exchange device (5), the first valve (120) is arranged on the bypass pipeline (110), and the second valve (130) is arranged between the input end of the heating furnace (6) and the input end of the bypass pipeline (110).
12. The hydrogenation heat exchange system according to any one of claims 1 to 3, wherein: the heat exchanger also comprises a fifth pipeline (140), a third valve (150) and a fourth valve (160), wherein the input end of the fifth pipeline (140) is connected with the mixing pipeline, and the output end of the fifth pipeline is connected with a second outlet connecting pipe (532) of a second cold medium channel of the second heat exchange device (5); the third valve (150) is disposed on the fifth line (140), and the fourth valve (160) is disposed between the input end of the fifth line (140) and the output end of the mixing line.
13. A heat exchange process for exchanging heat by using the hydrogenation heat exchange system as claimed in any one of claims 1 to 12, which is characterized by comprising the following steps:
inputting gas in a tenth pipeline (10) as a cold medium into a first heat exchange device (4), wherein the temperature of the gas in the tenth pipeline (10) is 60-80 ℃, the temperature of the gas discharged from the first heat exchange device (4) is 220-250 ℃, the gas is mixed with raw oil in the first pipeline (1), a mixture formed by the gas and the raw oil and bottom liquid of a stripping tower in a second pipeline (2) are used as the cold medium and are input into a second heat exchange device (5), the temperature of the raw oil in the first pipeline (1) is 160-210 ℃, and the temperature of the bottom liquid of the stripping tower in the second pipeline (2) is 220-250 ℃; and the mixture from the second heat exchange device (5) enters a hydrogenation reactor (7) for hydrogenation reaction and then is output from the hydrogenation reactor (7), the temperature of the output reaction product is 370-440 ℃, the reaction product is used as a heat medium of the second heat exchange device (5) to exchange heat with a cold medium in the second heat exchange device (5), the temperature of the reaction product from the second heat exchange device (5) is reduced to 250 ℃, the reaction product enters a heat high separation tank (8) to separate heat high-pressure gas and heat high-pressure oil, the separated heat high-pressure gas is used as a heat medium of the first heat exchange device (4) to exchange heat with the cold medium in the first heat exchange device (4), and then the heat high-pressure gas is output from the first heat exchange device (4).
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| CN115597402A (en) * | 2022-09-30 | 2023-01-13 | 镇海石化建安工程股份有限公司（Cn） | Heat exchange assembly for hydrogenation device and heat exchange process |
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