CN113091499A - 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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- CN113091499A CN113091499A CN202110478012.5A CN202110478012A CN113091499A CN 113091499 A CN113091499 A CN 113091499A CN 202110478012 A CN202110478012 A CN 202110478012A CN 113091499 A CN113091499 A CN 113091499A
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 73
- 238000000034 method Methods 0.000 title claims abstract description 27
- 239000000203 mixture Substances 0.000 claims abstract description 46
- 238000010438 heat treatment Methods 0.000 claims abstract description 42
- 238000000926 separation method Methods 0.000 claims abstract description 42
- 239000001257 hydrogen Substances 0.000 claims abstract description 24
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 24
- 239000007789 gas Substances 0.000 claims description 44
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- 229910001868 water Inorganic materials 0.000 claims description 38
- 239000007795 chemical reaction product Substances 0.000 claims description 32
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 17
- 238000004804 winding Methods 0.000 claims description 9
- 150000002431 hydrogen Chemical class 0.000 claims description 6
- 230000000694 effects Effects 0.000 abstract description 6
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- 239000000047 product Substances 0.000 description 8
- 239000002283 diesel fuel Substances 0.000 description 7
- 239000003507 refrigerant Substances 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- 239000002826 coolant Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 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
- 238000006243 chemical reaction Methods 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
- 238000001816 cooling Methods 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
- 238000004064 recycling Methods 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
Images
Classifications
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- 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) for conveying a mixture consisting of raw oil and hydrogen, a second pipeline (2) for conveying low-fraction oil, a heating furnace (6), a hydrogenation reactor (7), a hot high separation tank (8) and a heat exchange device (4), wherein the heat exchange device (4) comprises a first wound tube heat exchanger (4a) with a first heat medium channel (41) and at least two first cold medium channels, a second wound tube heat exchanger (4b) with a second heat medium channel (43) and at least one second cold medium channel (44) and a third wound tube heat exchanger (4c) with a third cold medium channel (45) and at least one third heat medium channel (46). 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 system comprises a first pipeline for conveying a mixture consisting of raw oil and hydrogen, a second pipeline for conveying low-fraction oil, a heating furnace, a hydrogenation reactor connected with the output end of the heating furnace, a high-temperature separation tank for separating a reaction product output by the hydrogenation reactor to obtain high-temperature gas and high-temperature fraction oil, and a heat exchange device, and is characterized in that:
the heat exchange device comprises a first wound tube type heat exchanger with a first heat medium channel and at least two first cold medium channels, a second wound tube type heat exchanger with a second heat medium channel and at least one second cold medium channel, and a third wound tube type heat exchanger with a third cold medium channel and at least one third heat medium channel;
the first winding pipe type 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 a 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 a first cold medium channel first, a first cold medium channel second inlet connecting pipe and a first cold medium channel second outlet connecting pipe which are communicated with a first cold medium channel second; 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 a second heat medium channel, and a second cold medium channel inlet connecting tube and a second cold medium channel outlet connecting tube which are communicated with a second cold medium channel; the third wound tube type heat exchanger is provided with a third cold medium channel inlet connecting tube and a third cold medium channel outlet connecting tube which are communicated with a third cold medium channel, and a third heat medium channel inlet connecting tube and a third heat medium channel outlet connecting tube which are communicated with a third heat medium channel;
an inlet connecting pipe of a first cold medium channel of the first wound tube type heat exchanger is connected with an output end of the first pipeline, an outlet connecting pipe of the first cold medium channel is connected with an inlet connecting pipe of a second cold medium channel of the second wound tube type heat exchanger, and an outlet connecting pipe of the second cold medium channel is connected with an input end of the heating furnace; the second heat medium channel inlet connecting pipe is connected with the output end of the hydrogenation reactor, the second heat medium channel outlet connecting pipe is connected with a third heat medium channel inlet connecting pipe of a third wound tube type heat exchanger, the third heat medium channel outlet connecting pipe is connected with the input end of the heat high separation tank, a heat high separation gas output end on the heat high separation tank for outputting heat high separation gas is connected with a first heat medium channel inlet connecting pipe in the first wound tube type heat exchanger, and the first heat medium channel outlet connecting pipe is connected to a second downstream device; and a second inlet connecting pipe of the first cold medium channel of the first wound tube type heat exchanger is connected with the output end of the second pipeline, a second outlet connecting pipe of the first cold medium channel is connected with a third inlet connecting pipe of the third cold medium channel of the third wound tube type heat exchanger, and an outlet connecting pipe of the third cold medium channel is connected to a first downstream device.
The first wound tube type heat exchanger is 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; and a third inlet connecting pipe of the first cold medium channel is connected with the output end of the fourth pipeline, and a third outlet connecting pipe of the first cold medium channel is connected to a third downstream device.
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 wound tube heat exchanger is a double-flow wound tube heat exchanger having one shell side and two tube sides. Alternatively, 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 wound tube heat exchanger is a wound tube heat exchanger having one tube side and two shell sides.
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 wound tube heat exchanger is a three-stream wound tube heat exchanger having one shell side and three tube sides. Alternatively, 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 wound tube heat exchanger is a wound tube heat exchanger having one tube side and three shell sides.
In each of the above solutions, 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 wound tube heat exchanger is a single-flow wound tube heat exchanger having one shell side and one tube side. Alternatively, the second heat medium channel may also be a tube side of the second wound tube heat exchanger, and the second cold medium channel is a shell side of the second wound tube heat exchanger.
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 also be a shell side of the third wound tube heat exchanger, and the third cold medium channel is a tube side of the third wound tube heat exchanger.
In each scheme, the system further comprises a third pipeline for conveying water, and a hot high-pressure gas output end of the hot high-pressure separation tank for outputting hot high-pressure gas is connected with an output end of the third pipeline and then connected with the first wound pipe type heat exchanger. 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.
Preferably, the second downstream equipment is a high-pressure air cooler;
or the downstream equipment II is a wound tube type 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 outlet connecting pipe of the first hot medium channel of the first wound tube type heat exchanger, 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.
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 wound tube heat exchanger, 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 system further comprises a fifth pipeline, a third valve and a fourth valve, wherein the input end of the fifth pipeline is connected with the second pipeline, and the output end of the fifth pipeline is connected with an outlet connecting pipe of a third cold medium channel of the third wound tube type heat exchanger; the third valve is arranged on a fifth pipeline, and the fourth valve is arranged between the input end of the fifth pipeline and the output end of the second pipeline.
Preferably, the system further comprises a sixth pipeline, a fifth valve and a sixth valve, wherein the input end of the sixth pipeline is connected with the first pipeline, and the output end of the sixth pipeline is connected between the input end of the heating furnace and the outlet connecting pipe of the second cold medium channel of the second wound tube type heat exchanger; the fifth valve is arranged on a sixth pipeline, and the sixth valve is arranged between the output end of the first pipeline and the input end of the sixth 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:
taking a mixture composed of raw oil and hydrogen in a first pipeline as a cold medium, sequentially passing through a first cold medium channel of a first wound tube type heat exchanger and a second cold medium channel of a second wound tube type heat exchanger, and then outputting the mixture from the second wound tube type heat exchanger, wherein the temperature of the mixture in the first pipeline is 70-165 ℃, the pressure is 4.5-19 MPa, and the temperature of the mixture from the second wound tube type heat exchanger is 320-395 ℃; the mixture discharged from the second wound tube type heat exchanger enters a hydrogenation reactor for hydrogenation reaction and then is output from the hydrogenation reactor, the temperature of the output reaction product is 355-420 ℃, the reaction product is taken as a heat medium and sequentially flows through a second heat medium channel of the second wound tube type heat exchanger and a third heat medium channel of the third wound tube type heat exchanger, the temperature of the reaction product discharged from the third wound tube type heat exchanger is reduced to 220-260 ℃, then the reaction product enters a heat high separation tank, heat high-pressure gas and heat high-pressure oil are separated out, and the separated heat high-pressure gas is taken as a heat medium, passes through a first heat medium channel of the first wound tube type heat exchanger and is output by the first wound tube type heat exchanger; and taking the low-fraction oil in the second pipeline as a cold medium, sequentially passing the low-fraction oil through the second first cold medium channel of the first wound tube type heat exchanger and the third cold medium channel of the third wound tube type heat exchanger, wherein the temperature of the low-fraction oil in the second pipeline is 45-65 ℃, the pressure is less than 2.5MPa, the temperature of the low-fraction oil discharged from the third wound tube type heat exchanger is 170-215 ℃, and sending the low-fraction oil to the first downstream equipment.
Compared with the prior art, the invention has the advantages that: the heat exchange device is designed into a first wound tube type heat exchanger with a first heat medium channel and at least two first cold medium channels, a second wound tube type heat exchanger with a second heat medium channel and at least one second cold medium channel, and a third wound tube type heat exchanger with a third cold medium channel and at least one third heat medium channel, 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 piping, the maintenance cost of the equipment and the like are reduced; in addition, the first, second and third wound tube heat exchangers are matched to realize and improve the heat exchange effect after the combination of a plurality of heat exchangers, the hydrogenation reaction can be carried out without a heating furnace after the operation is stable, and the temperature difference of a 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 view of a first wound tube heat exchanger according to a third embodiment of the present invention;
FIG. 4 is a schematic structural view of a first wound tube heat exchanger according to a fourth embodiment of the present invention;
fig. 5 is a schematic structural diagram of a fifth 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 first wound tube heat exchanger 4a, a second wound tube heat exchanger 4b, a third wound tube heat exchanger 4c, a heating furnace 6, a hydrogenation reactor 7, and a high thermal separation tank 8.
The first pipeline 1 is used for conveying a mixture consisting of raw oil and hydrogen, and the proportion of the raw oil and the hydrogen in the mixture is designed according to actual working conditions. The second line 2 is used for transporting the low fraction oil. The third line 3 is used for transporting water.
The input end of the hydrogenation reactor 7 is connected with the output end of the heating furnace 6, the thermal high separation tank 8 is used for separating the reaction product output by the hydrogenation reactor 7 to obtain thermal high-pressure gas and thermal high-pressure oil, the thermal high 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, the thermal high-pressure oil output by the thermal high-pressure oil output end 82 sequentially passes through the existing cold high-pressure separation tank and the cold low-pressure separation tank to obtain low-pressure oil, and the low-pressure oil can be input into the second pipeline 2.
The first wound tube heat exchanger 4a has one first heat medium channel 41 and two first cold medium channels, and the first wound tube heat exchanger 4a is provided with a first heat medium channel inlet connection pipe 411 and a first heat medium channel outlet connection pipe 412 which are communicated with the first heat medium channel 41, a first cold medium channel first inlet connection pipe 421 and a first cold medium channel first outlet connection pipe 422 which are communicated with the first cold medium channel first 42, and a first cold medium channel second inlet connection pipe 471 and a first cold medium channel second outlet connection pipe 472 which are communicated with the first cold medium channel second 47. In this embodiment, the first heat medium channel 41 is a shell side of the first wound tube heat exchanger 4a, the first cold medium channel is a tube side of the first wound tube heat exchanger 4a, and the first wound tube heat exchanger 4a is a double-flow wound tube heat exchanger having one shell side and two tube sides.
The second wound tube heat exchanger 4b has a second heat medium passage 43 and a second cold medium passage 44. The second wound tube heat exchanger 4b is provided with a second heat medium channel inlet connection pipe 431 and a second heat medium channel outlet connection pipe 432 which are communicated with the second heat medium channel 43, and a second cold medium channel inlet connection pipe 441 and a second cold medium channel outlet connection pipe 442 which are communicated with the second cold medium channel 44. In this embodiment, the second heat medium channel 43 is a shell side of the second wound tube heat exchanger 4b, the second cold medium channel 44 is a tube side of the second wound tube heat exchanger 4b, and the second wound tube heat exchanger 4b is a single-flow wound tube heat exchanger having one shell side and one tube side.
The third wound tube heat exchanger 4c has a third cooling medium passage 45 and a third heating medium passage 46. The third wound tube heat exchanger 4c is provided with a third refrigerant passage inlet connection pipe 451 and a third refrigerant passage outlet connection pipe 452 communicating with the third refrigerant passage 45, and a third heat medium passage inlet connection pipe 461 and a third heat medium passage outlet connection pipe 462 communicating with the third heat medium passage 46. In this embodiment, the third heat medium channel 46 is a tube side of the third wound tube heat exchanger 4c, the third cooling medium channel 45 is a shell side of the third wound tube heat exchanger 4c, and the third wound tube heat exchanger 4c is a single-flow wound tube heat exchanger having one shell side and one tube side.
The connection structure between each heat exchanger and each pipeline, heating furnace, hydrogenation reactor and thermal high separation tank in the embodiment is as follows:
a first cold medium channel inlet connecting pipe 421 of the first winding pipe type heat exchanger 4a is connected with the output end of the first pipeline 1, a first cold medium channel outlet connecting pipe 422 is connected with a second cold medium channel inlet connecting pipe 441 of the second winding pipe type heat exchanger 4b, and a second cold medium channel outlet connecting pipe 442 is connected with the input end of the heating furnace 6; a second heat medium channel inlet connecting pipe 431 is connected with the output end of the hydrogenation reactor 7, a second heat medium channel outlet connecting pipe 432 is connected with a third heat medium channel inlet connecting pipe 461 of a third wound tube type heat exchanger 4c, a third heat medium channel outlet connecting pipe 462 is connected with the input end of a heat high separation tank 8, a heat high gas output end 81 on the heat high separation tank 8 is connected with the output end of a third pipeline 3 and then is connected with a first heat medium channel inlet connecting pipe 411 in a first wound tube type heat exchanger 4a, and a first heat medium channel outlet connecting pipe 412 is connected with a second downstream device 9; the second inlet connection 471 of the first spiral-wound heat exchanger 4a is connected to the output of the second line 2, the second outlet connection 472 of the first spiral-wound heat exchanger 472 is connected to the third inlet connection 451 of the third spiral-wound heat exchanger 4c, and the third outlet connection 452 is connected to the first downstream device.
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-pressure air separation tank to separate out a gas containing hydrogen, and the gas can be input into the first pipeline 1 for recycling. The first downstream device may be a separation column, not shown.
The method for exchanging heat by adopting the hydrogenation heat exchange system of the embodiment comprises the following steps:
the method comprises the following steps of (1) sequentially enabling a mixture consisting of raw oil and hydrogen in a first pipeline 1 to pass through one tube pass of a first wound tube type heat exchanger 4a and a tube pass of a second wound tube type heat exchanger 4b and then outputting the mixture from the second wound tube type heat exchanger 4b, wherein the temperatures of the raw oil and the hydrogen in the first pipeline 1 are 70 ℃ and 83.4 ℃, and the temperature of the mixture from the second wound tube type heat exchanger 4b is 330-388 ℃; the mixture from the second wound tube type heat exchanger 4b passes through a heating furnace 6 and a hydrogenation reactor 7 and then is output from the hydrogenation reactor 7, the temperature of the output reaction product is 370-415 ℃, the reaction product is used as a heat medium and sequentially flows through the shell pass of the second wound tube type heat exchanger 4b and the tube pass of the third wound tube type heat exchanger 3c, the temperature of the reaction product from the tube pass of the third wound tube type heat exchanger 3c is reduced to 230 ℃, then the reaction product enters a thermal high separation tank 8, thermal high-pressure gas and thermal high-pressure oil are separated out, the separated thermal high-pressure gas is mixed with water in the third pipeline 3 and then flows through the shell pass of the first wound tube type heat exchanger 4a, the temperature of the thermal high-pressure gas and the water from the shell pass of the first wound tube type heat exchanger 4a is reduced to 105 ℃, and then the mixture enters a second downstream device 9. And the low-fraction oil in the second pipeline 2 sequentially flows through the other tube pass of the first wound tube type heat exchanger 4a and the shell pass of the third wound tube type heat exchanger 4c, the temperature of the low-fraction oil in the second pipeline 2 is 55 ℃, the temperature of the low-fraction oil discharged from the shell pass of the third wound tube type heat exchanger 4c is 185-207 ℃, and the low-fraction oil is sent to the first downstream equipment.
Example two:
as shown in fig. 2, 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 is basically the same as the first embodiment, except that the first wound tube heat exchanger 4a in this embodiment is slightly different from the first embodiment, the first wound tube heat exchanger 4a in this embodiment has one first heat medium channel 41 and three first cold medium channels, and the first wound tube heat exchanger 4a is further provided with a first cold medium channel three-inlet connection pipe 481 and a first cold medium channel three-outlet connection pipe 482 which are communicated with a first cold medium channel three 48. In this embodiment, the first wound tube heat exchanger 4a is a three-stream wound tube heat exchanger having one shell side and three tube sides.
Meanwhile, the present embodiment further includes a fourth line 30 for delivering water, a first cold medium channel three inlet connection 481 is connected to an output end of the fourth line 30, and a first cold medium channel three outlet connection 482 is connected to a downstream device three. In this manner, the water in the fourth line 30 may be heated. And the downstream equipment three can be equipment needing hot water or a pipeline for conveying hot water, in the embodiment, the hot water from the outlet connection 482 of the first cold medium channel three can be conveyed into the third pipeline 3.
The method for exchanging heat by adopting the hydrogenation heat exchange system of the embodiment comprises the following steps:
the mixture in the first pipeline 1 sequentially passes through one tube pass of the first wound tube type heat exchanger 4a and the tube pass of the second wound tube type heat exchanger 4b and then is output from the second wound tube type heat exchanger 4b, the temperature of the mixture in the first pipeline 1 is 130 ℃, and the temperature of the mixture from the second wound tube type heat exchanger 4b is 330-388 ℃; the mixture from the second wound tube type heat exchanger 4b passes through a heating furnace 6 and a hydrogenation reactor 7 and then is output from the hydrogenation reactor 7, the temperature of the output reaction product is 370-415 ℃, the reaction product is used as a heat medium and sequentially flows through the shell pass of the second wound tube type heat exchanger 4b and the tube pass of the third wound tube type heat exchanger 3c, the temperature of the reaction product from the tube pass of the third wound tube type heat exchanger 3c is reduced to 230 ℃, then the reaction product enters a thermal high separation tank 8, thermal high-pressure gas and thermal high-pressure oil are separated out, the separated thermal high-pressure gas is mixed with water in the third pipeline 3 and then flows through the shell pass of the first wound tube type heat exchanger 4a, the temperature of the thermal high-pressure gas and the water from the shell pass of the first wound tube type heat exchanger 4a is reduced to 95 ℃, and then the mixture enters a second downstream device 9. And the low-fraction oil in the second pipeline 2 sequentially flows through the other tube pass of the first wound tube type heat exchanger 4a and the shell pass of the third wound tube type heat exchanger 4c, the temperature of the low-fraction oil in the second pipeline 2 is 55 ℃, the temperature of the low-fraction oil discharged from the shell pass of the third wound tube type heat exchanger 4c is 185-207 ℃, and the low-fraction oil is sent to the first downstream equipment. The water in the fourth line 30 is fed into the last tube pass of the first wound tube heat exchanger 4a, the temperature of the water in the fourth line 30 is 70 ℃, the temperature of the water coming out of the first wound tube heat exchanger 4a is 95 ℃, and the water is sent to the third downstream equipment.
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 basically the same as the first embodiment, except that the first wound tube heat exchanger 4a in the present embodiment is slightly different from the first wound tube heat exchanger in the first embodiment, in the present embodiment, the first heat medium channel 41 is a tube side of the first wound tube heat exchanger 4a, the first cold medium channel is a shell side of the first wound tube heat exchanger 4a, and the first wound tube heat exchanger 4a is a wound tube heat exchanger having two shell sides and one tube side.
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 second embodiment, except that the first wound tube heat exchanger 4a in the present embodiment is slightly different from the first wound tube heat exchanger in the second embodiment, in the present embodiment, the first heat medium channel 41 is a tube side of the first wound tube heat exchanger 4a, the first cold medium channel is a shell side of the first wound tube heat exchanger 4a, and the first wound tube heat exchanger 4a is a wound tube heat exchanger having three shell sides and one tube side.
Example five:
as shown in fig. 5, a fifth preferred embodiment of the hydrogenation heat exchange system and the heat exchange process using a multi-stream wound tube heat exchanger according to the present invention is basically the same as the hydrogenation heat exchange system in the first embodiment, except that the downstream equipment two 9 in this embodiment is a wound tube heat exchanger having a heat medium channel 92 and a cold medium channel 91. The hydrogenation heat exchange system of this embodiment further includes a cold water pipeline 100 for conveying 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 inlet connection pipe of the heat medium channel 92 of the second downstream equipment 9 is connected to the first heat medium channel outlet connection pipe 412 of the first coiled pipe heat exchanger 4a, and an outlet connection pipe of the heat medium channel 92 is connected to the cold high separation tank 93.
Meanwhile, the hydrogenation heat exchange system of the embodiment further includes a bypass line 110, a first valve 120, a second valve 130, a fifth line 140, a third valve 150, a fourth valve 160, a sixth line 170, a fifth valve 180, and a sixth valve 190. The output end of the bypass line 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 line 110 is connected between the input end of the heating furnace 6 and the second cooling medium passage outlet connection pipe 442 of the second wound tube heat exchanger 4b, the first valve 120 is arranged on the bypass line 110, and the second valve 130 is arranged between the input end of the heating furnace 6 and the input end of the bypass line 110. The input end of the fifth pipeline 140 is connected to the second pipeline 2, and the output end is connected to the third refrigerant passage outlet connection pipe 452 of the third wound tube heat exchanger 4 c; 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 second line 2. The input end of the sixth pipeline 170 is connected to the first pipeline 1, and the output end is connected between the input end of the heating furnace 6 and the outlet connection pipe 442 of the second refrigerant passage of the second wound tube heat exchanger 4 b; a fifth valve 180 is provided on the sixth line 170, and a sixth valve 190 is provided between the output end of the first line 1 and the input end of the sixth line 170. The bypass line 110, the fifth line 140, the sixth line 170 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 heat exchange by adopting the hydrogenation heat exchange system of the embodiment comprises the following steps:
taking a mixture composed of raw oil and hydrogen in a first pipeline 1 as a cold medium, sequentially passing through a first cold medium channel 42 of a first wound tube type heat exchanger 4a and a second cold medium channel 44 of a second wound tube type heat exchanger 4b, and then outputting the mixture from the second wound tube type heat exchanger 4b, wherein the temperature of the mixture in the first pipeline 1 is 130 ℃, the pressure is 4.5-19 MPa, and the temperature of the mixture from the second wound tube type heat exchanger 4b is 330-388 ℃; the mixture from the second wound tube type heat exchanger 4b 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 370-415 ℃, the reaction product as a heat medium sequentially passes through a second heat medium channel 43 of the second wound tube type heat exchanger 4b and a third heat medium channel 46 of the third wound tube type heat exchanger 4c, the temperature of the reaction product from the third wound tube type heat exchanger 4c is reduced to 230 ℃, then the reaction product enters a thermal high separation tank 8 for separating thermal high-pressure gas and thermal high-pressure oil, the separated thermal high-pressure gas as a heat medium passes through a first heat medium channel 41 of the first wound tube type heat exchanger 4a and is output by the first wound tube type heat exchanger 4a, the temperature of the output medium is 105 ℃, then the mixture enters a heat medium channel 92 of a second downstream device 9, cold water (the water temperature is lower than 35 ℃) in a cold water pipeline 100 is input into a cold medium channel 91 of the second downstream device 9, the temperature of water from a cold medium channel 91 of the second downstream equipment 9 is less than 45 ℃, the temperature of a medium from a hot medium channel 92 of the second downstream equipment 9 is 50 ℃, and the water is sent into a cold high separation tank for separation; meanwhile, the low-fraction oil in the second pipeline 2 is taken as a cold medium to sequentially flow through the second first cold medium channel 47 of the first wound tube type heat exchanger 4a and the third cold medium channel 45 of the third wound tube type heat exchanger 4c, the temperature of the low-fraction oil in the second pipeline 2 is 55 ℃, the pressure is less than 2.5MPa, the temperature of the low-fraction oil from the third wound tube type heat exchanger 4c is 185-plus-207 ℃, and the low-fraction oil is sent to the first downstream equipment.
The hydrogenation heat exchange system of this embodiment is because heat exchange efficiency is high for the mixture that comes out from second winding tubular heat exchanger 4b need not the heating furnace heating and just can directly get into hydrogenation ware 7 and react, and the heating furnace only needs to use at the operation initial stage, and bypass line 110 can all be walked to other operation stages.
Example six:
the technical scheme of this embodiment is basically the same as that of the first embodiment, except that the heat exchange process is slightly different, and the method for exchanging heat by using the hydrogenation heat exchange system of this embodiment is as follows:
the mixture composed of raw oil and hydrogen in the first pipeline 1 sequentially passes through one tube pass of the first wound tube type heat exchanger 4a and the tube pass of the second wound tube type heat exchanger 4b and then is output from the second wound tube type heat exchanger 4b, the temperature of the mixture in the first pipeline 1 is 70 ℃, the pressure is 4.5MPa, and the temperature of the mixture output from the second wound tube type heat exchanger 4b is 320 ℃; the mixture from the second wound tube type heat exchanger 4b passes through a heating furnace 6 and a hydrogenation reactor 7 and then is output from the hydrogenation reactor 7, the temperature of the output reaction product is 355 ℃, the reaction product as a heat medium sequentially passes through the shell pass of the second wound tube type heat exchanger 4b and the tube pass of the third wound tube type heat exchanger 3c, the temperature of the reaction product from the tube pass of the third wound tube type heat exchanger 3c is reduced to 220 ℃, then the reaction product enters a thermal high separation tank 8, thermal high-pressure gas and thermal high-pressure oil are separated out, the separated thermal high-pressure gas is mixed with water in the third pipeline 3 and then passes through the shell pass of the first wound tube type heat exchanger 4a, the temperature of the thermal high-pressure gas and the water from the shell pass of the first wound tube type heat exchanger 4a is reduced to 105 ℃, and then the mixture enters a second downstream device 9. And (3) sequentially feeding the low-fraction oil in the second pipeline 2 through the other tube pass of the first wound tube type heat exchanger 4a and the shell pass of the third wound tube type heat exchanger 4c, wherein the temperature of the low-fraction oil in the second pipeline 2 is 45 ℃, the pressure is 2.0MPa, the temperature of the low-fraction oil discharged from the shell pass of the third wound tube type heat exchanger 4c is 170 ℃, and the low-fraction oil is sent to the first downstream equipment.
Example seven:
the technical scheme of this embodiment is basically the same as that of the first embodiment, except that the heat exchange process is slightly different, and the method for exchanging heat by using the hydrogenation heat exchange system of this embodiment is as follows:
the mixture composed of raw oil and hydrogen in the first pipeline 1 sequentially passes through one tube pass of the first wound tube type heat exchanger 4a and the tube pass of the second wound tube type heat exchanger 4b and then is output from the second wound tube type heat exchanger 4b, the temperature of the mixture in the first pipeline 1 is 165 ℃, the pressure is 19MPa, and the temperature of the mixture output from the second wound tube type heat exchanger 4b is 395 ℃; the mixture from the second wound tube type heat exchanger 4b passes through a heating furnace 6 and a hydrogenation reactor 7 and then is output from the hydrogenation reactor 7, the temperature of the output reaction product is 420 ℃, the reaction product is taken as a heat medium and sequentially flows through the shell pass of the second wound tube type heat exchanger 4b and the tube pass of the third wound tube type heat exchanger 3c, the temperature of the reaction product from the tube pass of the third wound tube type heat exchanger 3c is reduced to 260 ℃, then the reaction product enters a thermal high separation tank 8, thermal high-pressure gas and thermal high-pressure oil are separated out, the separated thermal high-pressure gas is mixed with water in the third pipeline 3 and then flows through the shell pass of the first wound tube type heat exchanger 4a, the temperature of the thermal high-pressure gas and the water from the shell pass of the first wound tube type heat exchanger 4a is reduced to 105 ℃, and then the mixture enters a second downstream device 9. And (3) sequentially feeding the low-fraction oil in the second pipeline 2 through the other tube pass of the first wound tube type heat exchanger 4a and the shell pass of the third wound tube type heat exchanger 4c, wherein the temperature of the low-fraction oil in the second pipeline 2 is 65 ℃, the pressure is 1.5MPa, and the temperature of the low-fraction oil discharged from the shell pass of the third wound tube type heat exchanger 4c is 215 ℃, and sending the low-fraction oil to the first downstream equipment.
The temperatures of the raw oil, the hydrogen and the low-temperature oil 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 be reduced, the whole structure is simple, and the implementation is convenient.
Claims (12)
1. A hydronic heat exchange system employing a multi-stream wound tube heat exchanger, comprising: the device comprises a first pipeline (1) for conveying a mixture consisting of raw oil and hydrogen, a second pipeline (2) for conveying low-fraction oil, a heating furnace (6), a hydrogenation reactor (7) connected with the output end of the heating furnace (6), a high-temperature separation tank (8) for separating a reaction product output by the hydrogenation reactor (7) to obtain high-temperature gas and high-temperature oil, and a heat exchange device (4), and is characterized in that:
the heat exchange device (4) comprises a first wound tube heat exchanger (4a) with a first heat medium channel (41) and at least two first cold medium channels, a second wound tube heat exchanger (4b) with a second heat medium channel (43) and at least one second cold medium channel (44), a third wound tube heat exchanger (4c) with a third cold medium channel (45) and at least one third heat medium channel (46);
the first wound tube type heat exchanger (4a) 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 a 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 a first cold medium channel first (42), and a first cold medium channel second inlet connecting pipe (471) and a first cold medium channel second outlet connecting pipe (472) which are communicated with a first cold medium channel second (47); a second heat medium channel inlet connecting pipe (431) and a second heat medium channel outlet connecting pipe (432) which are communicated with a second heat medium channel (43), a second cold medium channel inlet connecting pipe (441) and a second cold medium channel outlet connecting pipe (442) which are communicated with a second cold medium channel (44) are arranged on the second wound tube type heat exchanger (4 b); a third cold medium channel inlet connecting pipe (451) and a third cold medium channel outlet connecting pipe (452) which are communicated with a third cold medium channel (45), a third heat medium channel inlet connecting pipe (461) and a third heat medium channel outlet connecting pipe (462) which are communicated with a third heat medium channel (46) are arranged on the third wound tube type heat exchanger (4 c);
a first cold medium channel inlet connecting pipe (421) of the first wound tube heat exchanger (4a) is connected with the output end of the first pipeline (1), a first cold medium channel outlet connecting pipe (422) of the first wound tube heat exchanger (4a) is connected with a second cold medium channel inlet connecting pipe (441) of the second wound tube heat exchanger (4b), and a second cold medium channel outlet connecting pipe (442) of the first wound tube heat exchanger is connected with the input end of the heating furnace (6); the second heat medium channel inlet connecting pipe (431) is connected with the output end of the hydrogenation reactor (7), the second heat medium channel outlet connecting pipe (432) is connected with a third heat medium channel inlet connecting pipe (461) of the third wound tube type heat exchanger (4c), the third heat medium channel outlet connecting pipe (462) is connected with the input end of the high-temperature separation tank (8), a high-temperature gas output end (81) of the high-temperature separation tank (8) for outputting high-temperature gas is connected with a first heat medium channel inlet connecting pipe (411) in the first wound tube type heat exchanger (4a), and the first heat medium channel outlet connecting pipe (412) is connected to a second downstream device (9); a first cold medium channel second inlet connecting pipe (471) of the first winding pipe type heat exchanger (4a) is connected with the output end of the second pipeline (2), a first cold medium channel second outlet connecting pipe (472) is connected with a third cold medium channel inlet connecting pipe (451) of the third winding pipe type heat exchanger (4c), and a third cold medium channel outlet connecting pipe (452) is connected to a first downstream device.
2. The hydrogenation heat exchange system of claim 1, wherein: the water-cooled heat exchanger further comprises a fourth pipeline (30) for conveying water, at least three first cold medium channels in the first wound tube type heat exchanger (4a) are provided, and a first cold medium channel three-inlet connecting pipe (481) and a first cold medium channel three-outlet connecting pipe (482) which are communicated with the first cold medium channel three (48) are further arranged on the first wound tube type heat exchanger (4 a); the first cold medium channel three inlet connection (481) is connected with the output end of the fourth pipeline (30), and the first cold medium channel three outlet connection (482) is connected with a downstream device three.
3. The hydrogenation heat exchange system of claim 1, wherein: the first heat medium channel (41) is a shell side of the first wound tube heat exchanger (4a), the first cold medium channel is a tube side of the first wound tube heat exchanger (4a), and the first wound tube heat exchanger (4a) is a double-flow wound tube heat exchanger having one shell side and two tube sides.
4. The hydrogenation heat exchange system of claim 2, wherein: the first heat medium channel (41) is a shell side of the first wound tube heat exchanger (4a), the first cold medium channel is a tube side of the first wound tube heat exchanger (4a), and the first wound tube heat exchanger (4a) is a three-stream wound tube heat exchanger having one shell side and three tube sides.
5. A hydrogenation heat exchange system according to any one of claims 1 to 4, wherein: the second heat medium channel (43) is a shell side of the second wound tube heat exchanger (4b), the second cold medium channel (44) is a tube side of the second wound tube heat exchanger (4b), and the second wound tube heat exchanger (4b) is a single-flow wound tube heat exchanger having one shell side and one tube side.
6. A hydrogenation heat exchange system according to any one of claims 1 to 4, wherein: the third heat medium channel (46) is a tube side of the third wound tube heat exchanger (4c), the third cold medium channel (45) is a shell side of the third wound tube heat exchanger (4c), and the third wound tube heat exchanger (4c) is a single-flow wound tube heat exchanger having one shell side and one tube side.
7. A hydrogenation heat exchange system according to any one of claims 1 to 4, wherein: the high-temperature gas separation device is characterized by further comprising a third pipeline (3) used for conveying water, wherein a high-temperature gas separation output end (81) of the high-temperature separation tank (8) used for outputting high-temperature gas is connected with the output end of the third pipeline (3) and then connected with the first wound tube type heat exchanger (4 a).
8. A hydrogenation heat exchange system according to any one of claims 1 to 4, wherein: the second downstream equipment (9) is a high-pressure air cooler;
or the downstream equipment II (9) is a winding tube type heat exchanger with a hot 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 hot medium channel (92) of the downstream equipment II (9) is connected with the first hot medium channel outlet connecting pipe (412) of the first winding tube type heat exchanger (4a), and the outlet of the hot medium channel (92) is connected to the cold high separation tank (93).
9. A hydrogenation heat exchange system according to any one of claims 1 to 4, wherein: the device 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 the outlet connecting pipe (442) of the second cold medium channel of the second wound tube type heat exchanger (4b), 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).
10. A hydrogenation heat exchange system according to any one of claims 1 to 4, wherein: the system 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 second pipeline (2), and the output end of the fifth pipeline is connected with a third cold medium channel outlet connecting pipe (452) of the third wound tube type heat exchanger (4 c); the third valve (150) is arranged on the fifth pipeline (140), and the fourth valve (160) is arranged between the input end of the fifth pipeline (140) and the output end of the second pipeline (2).
11. A hydrogenation heat exchange system according to any one of claims 1 to 4, wherein: the system also comprises a sixth pipeline (170), a fifth valve (180) and a sixth valve (190), wherein the input end of the sixth pipeline (170) is connected with the first pipeline (1), and the output end of the sixth pipeline is connected between the input end of the heating furnace (6) and a second cold medium channel outlet connecting pipe (442) of the second wound tube type heat exchanger (4 b); the fifth valve (180) is arranged on a sixth pipeline (170), and the sixth valve (190) is arranged between the output end of the first pipeline (1) and the input end of the sixth pipeline (170).
12. A heat exchange process for exchanging heat by using the hydrogenation heat exchange system as claimed in any one of claims 1 to 11, which is characterized by comprising the following steps:
taking a mixture composed of raw oil and hydrogen in a first pipeline (1) as a cold medium, sequentially passing through a first cold medium channel (42) of a first wound tube type heat exchanger (4a) and a second cold medium channel (44) of a second wound tube type heat exchanger (4b), and then outputting the mixture from the second wound tube type heat exchanger (4b), wherein the temperature of the mixture in the first pipeline (1) is 70-165 ℃, the pressure is 4.5-19 MPa, and the temperature of the mixture from the second wound tube type heat exchanger (4b) is 320-395 ℃; the mixture discharged from the second wound tube type heat exchanger (4b) 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 355-420 ℃, the reaction product as a heat medium sequentially passes through a second heat medium channel (43) of the second wound tube type heat exchanger (4b) and a third heat medium channel (46) of a third wound tube type heat exchanger (4c), the temperature of the reaction product discharged from the third wound tube type heat exchanger (4c) is reduced to 220-260 ℃, and then the reaction product enters a heat high separation tank (8), heat high-pressure gas and heat high-pressure oil are separated out, the separated heat high-pressure gas as the heat medium passes through a first heat medium channel (41) of the first wound tube type heat exchanger (4a), and is output from the first wound tube type heat exchanger (4 a); and taking the low-fraction oil in the second pipeline (2) as a cold medium to sequentially pass through a second cold medium channel (47) of the first wound tube type heat exchanger (4a) and a third cold medium channel (45) of the third wound tube type heat exchanger (4c), wherein the temperature of the low-fraction oil in the second pipeline (2) is 45-65 ℃, the pressure is less than 2.5MPa, the temperature of the low-fraction oil discharged from the third wound tube type heat exchanger (4c) is 170-215 ℃, and the low-fraction oil is sent to a first downstream device.
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| CN113091498A (en) * | 2021-04-30 | 2021-07-09 | 镇海石化建安工程有限公司 | Hydrogenation heat exchange system and heat exchange process adopting multi-strand wound tube type heat exchanger |
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Address after: 315207 Jiaochuan Street Refining Road, Zhenhai District, Ningbo City, Zhejiang Province Applicant after: Zhenhai Petrochemical Construction and Installation Engineering Co.,Ltd. Address before: 315207 Jiaochuan Street Refining Road, Zhenhai District, Ningbo City, Zhejiang Province Applicant before: ZHENHAI PETROCHEMICAL JIANAN ENGINEERING Co.,Ltd. |
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| CB02 | Change of applicant information |