CN113091499B - Hydrogenation heat exchange system and heat exchange process adopting multi-strand winding tubular heat exchanger - Google Patents
Hydrogenation heat exchange system and heat exchange process adopting multi-strand winding tubular heat exchanger Download PDFInfo
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- CN113091499B CN113091499B CN202110478012.5A CN202110478012A CN113091499B CN 113091499 B CN113091499 B CN 113091499B CN 202110478012 A CN202110478012 A CN 202110478012A CN 113091499 B CN113091499 B CN 113091499B
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000004804 winding Methods 0.000 title claims description 153
- 238000010438 heat treatment Methods 0.000 claims abstract description 47
- 239000000203 mixture Substances 0.000 claims abstract description 37
- 238000000926 separation method Methods 0.000 claims abstract description 37
- 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 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 36
- 229910001868 water Inorganic materials 0.000 claims description 36
- 239000007795 chemical reaction product Substances 0.000 claims description 35
- 239000002826 coolant Substances 0.000 claims description 28
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 18
- 150000002431 hydrogen Chemical class 0.000 claims description 5
- 230000000694 effects Effects 0.000 abstract description 6
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- 210000002445 nipple Anatomy 0.000 description 8
- 239000000047 product Substances 0.000 description 6
- 239000002283 diesel fuel Substances 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000003209 petroleum derivative Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound 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
- 238000001816 cooling 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 compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000004891 communication 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
- 239000002184 metal Substances 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 Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
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
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
A hydrogenation heat exchange system comprising: a first line (1) for transporting a mixture consisting of feedstock oil and hydrogen, a second line (2) for transporting low-split oil, a heating furnace (6), a hydrogenation reactor (7), a heat high separation tank (8), and a heat exchange device (4), the heat exchange device (4) comprising a first wound tube heat exchanger (4 a) with one first heat medium channel (41) and at least two first cold medium channels, a second wound tube heat exchanger (4 b) with one second heat medium channel (43) and at least one second cold medium channel (44), a third wound tube heat exchanger (4 c) with one third cold medium channel (45) and at least one third heat medium channel (46). The application also discloses a heat exchange process for carrying out heat exchange by adopting the hydrogenation heat exchange system. Compared with the prior art, the application can reduce the number of heat exchangers, improve the heat exchange effect and reduce the pressure drop of the system.
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-flow winding tube type heat exchanger.
Background
Hydrotreating is one of the more important treatment methods in petroleum products, namely, under the conditions of a certain temperature, hydrogen partial pressure and catalyst, heteroatoms such as sulfur, nitrogen, oxygen and the like and metal impurities in the petroleum products are removed, and olefin is saturated and aromatic hydrocarbon is partially hydrogenated and saturated, so that the usability of the petroleum products is improved.
The hydrotreating process is as follows: mixing the oil product with hydrogen, heating to a specified temperature in a heating furnace, and then entering a reactor filled with a catalyst; after the reaction is finished, hydrogen is separated in a separator and recycled through a compressor; the product is separated from hydrogen sulfide, ammonia, water and gaseous hydrogen produced by small amount of decomposition during the reaction in a stabilizer.
The prior heat exchange process for hydrogenation is disclosed in the invention patent application No. CN201310344264.4 (application publication No. CN 103421542A), which comprises the following steps: 1) The diesel oil and the hydrogen are mixed and then enter a first heat exchanger for heat exchange, and the temperature is raised to 270-280 ℃; 2) Feeding the mixture from the first heat exchanger into a raw material heating furnace, heating to 320-330 ℃, and feeding into a hydrogenation reactor; 3) The reaction product from the hydrogenation reactor is cooled to 175-185 ℃ after sequentially exchanging heat by a fifth heat exchanger, a first heat exchanger and a second heat exchanger, then injected with water and cooled to 45-55 ℃ by a first air cooler, and then enters a cold high-pressure separation tank to separate hydrogen-containing gas and cold high-pressure separation oil; 4) The 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, is divided into two paths after being mixed, wherein one path is mixed with diesel oil, the other path is fed into a hydrogenation reactor, and cold high-pressure separation oil discharged from the cold high-pressure separation tank is fed into a cold low-pressure separation tank after being depressurized, and low-pressure separation gas and low-pressure separation oil are separated from the cold low-pressure separation tank; 5) The low-pressure gas is discharged from the cold low-pressure tank, and the low-pressure oil is subjected to heat exchange sequentially through a second heat exchanger, a third heat exchanger and a fifth heat exchanger and then enters a stripping fractionating tower, at the moment, stripping steam is injected into the stripping fractionating tower, and then naphtha, sulfur-containing oil gas and product diesel oil are separated from the stripping fractionating tower; 6) And (3) delivering naphtha and sulfur-containing oil gas to the next procedure after exiting the stripping fractionating tower, and enabling the product diesel oil to pass through a third heat exchanger and a fourth heat exchanger in sequence, then cooling the product diesel oil in a second air cooler, and finally entering a finished product tank area after cooling to 45-55 ℃.
The equipment adopted in the hydrogenation process is high-temperature and high-pressure equipment due to harsh operation conditions, the conventional heat exchangers are difficult to produce in a large scale, and the same number in the prior art can only adopt a mode of connecting a plurality of heat exchangers in series/parallel to meet the process requirements along with the expansion of the scale of the equipment, so that the cost is obviously 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 capable of reducing the number of heat exchangers and improving the heat exchange effect at the same time aiming at the current state of the art.
The second technical problem to be solved by the invention is to provide a heat exchange process for heat exchange by adopting 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 hydro-heat exchange system employing a multi-stream wound tube heat exchanger, comprising: the hydrogenation device comprises a first pipeline for conveying a mixture composed of raw oil and hydrogen, a second pipeline for conveying low-pressure oil, a heating furnace, a hydrogenation reactor connected with the output end of the heating furnace, a thermal high-separation tank for separating reaction products output by the hydrogenation reactor to obtain thermal high-pressure gas and thermal high-pressure oil, and a heat exchange device, and is characterized in that:
the heat exchange device comprises a first wound tube heat exchanger with one first heat medium channel and at least two first cold medium channels, a second wound tube heat exchanger with one second heat medium channel and at least one second cold medium channel, and a third wound tube heat exchanger with one third cold medium channel and at least one third heat medium channel;
The first winding tube type heat exchanger is provided with a first heat medium channel inlet connecting tube and a first heat medium channel outlet connecting tube which are communicated with a first heat medium channel, a first cold medium channel first inlet connecting tube and a first cold medium channel first outlet connecting tube which are communicated with a first cold medium channel first, and a first cold medium channel second inlet connecting tube and a first cold medium channel second outlet connecting tube which are communicated with a first cold medium channel second; the second winding 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 winding 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 winding tube type heat exchanger is connected with the 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 winding tube type heat exchanger, and an outlet connecting pipe of the second cold medium channel is connected with the 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 the third heat medium channel inlet connecting pipe of the third winding pipe type heat exchanger, the third heat medium channel outlet connecting pipe is connected with the input end of the heat high separation tank, the heat high separation tank is provided with a heat high-pressure gas output end for outputting heat high-pressure gas, the heat high-pressure gas output end is connected with the first heat medium channel inlet connecting pipe in the first winding pipe type heat exchanger, and the first heat medium channel outlet connecting pipe is connected to downstream equipment II; the second inlet connecting pipe of the first cooling medium channel of the first winding tube type heat exchanger is connected with the output end of the second pipeline, the second outlet connecting pipe of the first cooling medium channel is connected with the third inlet connecting pipe of the third cooling medium channel of the third winding tube type heat exchanger, and the third outlet connecting pipe of the cooling medium channel is connected to the first downstream equipment.
Further, the heat exchanger further comprises a fourth pipeline for conveying water, at least three first cold medium channels are arranged in the first winding tube type heat exchanger, and the first winding tube type heat exchanger 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 cooling medium channel is connected with the output end of the fourth pipeline, and the third outlet connecting pipe of the first cooling medium channel is connected to the third downstream equipment.
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 with one shell side and two tube sides. Alternatively, the first heat medium channel may be a tube side of a 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-flow wound tube heat exchanger with one shell side and three tube sides. Alternatively, the first heat medium channel may 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 embodiments, 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 be a tube side of the second wound tube heat exchanger, and the second cooling medium channel may be 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 with 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 cooling medium channel may be a tube side of the third wound tube heat exchanger.
In each scheme, the device further comprises a third pipeline for conveying water, wherein the hot high-pressure separation tank is used for outputting hot high-pressure gas, and the hot high-pressure gas output end of the hot high-pressure separation tank is connected with the output end of the third pipeline and then connected with the first winding pipe type heat exchanger. Thus, water can dissolve partial mediums such as hydrogen sulfide, ammonium salt and the like in the hot high-pressure gas, so that the phenomenon that the partial mediums in the hot high-pressure gas corrode a heat exchanger is reduced.
Preferably, the second downstream device is a high-pressure air cooler;
Or, the second downstream equipment is a winding tube type heat exchanger with one heat medium channel and at least one cold medium channel, and further comprises a cold water pipeline for conveying cold water, wherein the output end of the cold water pipeline is connected with an inlet connecting tube of the cold medium channel of the second downstream equipment, the inlet connecting tube of the heat medium channel of the second downstream equipment is connected with a first heat medium channel outlet connecting tube of the first winding tube type heat exchanger, and an outlet connecting tube of the heat medium channel is connected to a cold high separation tank.
The coiled tube type heat exchanger can be used for replacing the high-pressure air cooler, a hydrogenation device usually needs a plurality of high-pressure air coolers, the size of each air cooler is about 10.5 x 3m, the volume is larger, and the occupied area is larger; 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 hydrogenation reactor further comprises a bypass pipeline, a first valve and a second valve, wherein the output end of the bypass pipeline is connected between the output end of the heating furnace and the input end of the hydrogenation reactor, the input end of the bypass pipeline is connected between the input end of the heating furnace and the second cold medium channel outlet connecting pipe of the second winding pipe type heat exchanger, the first valve is arranged on the bypass pipeline, and the second valve is arranged between the input end of the heating furnace and the input end of the bypass pipeline. Namely, the heating furnace is a start-up heating furnace, heating work is only needed in the start-up stage (namely, the initial stage of system operation), and the rest stages do not need to work. The heat exchange device mainly has the advantages that better heat exchange effect can be achieved, the operation load of the heating furnace can be greatly reduced, and the heating furnace with smaller volume and smaller heating capacity can be used.
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 second pipeline, and the output end of the fifth pipeline is connected with a third cold medium channel outlet connecting pipe of the third winding pipe type 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 second pipeline.
Preferably, the heating furnace 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 second cold medium channel outlet connecting pipe of the second winding pipe type heat exchanger; the fifth valve is arranged on the 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 invention solves the second technical problem by adopting the technical proposal that: the heat exchange process for carrying out heat exchange by adopting the hydrogenation heat exchange system is characterized by comprising the following steps:
The method comprises the steps of sequentially passing a mixture consisting of raw oil and hydrogen in a first pipeline through a first cold medium channel of a first winding tube heat exchanger and a second cold medium channel of a second winding tube heat exchanger as cold media and then outputting the mixture from the second winding tube 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 discharged from the second winding tube heat exchanger is 320-395 ℃; the mixture from the second winding 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 sequentially goes through a second heat medium channel of the second winding tube type heat exchanger and a third heat medium channel of a third winding tube type heat exchanger as heat mediums, the temperature of the reaction product from the third winding tube type heat exchanger is reduced to 220-260 ℃, then the reaction product enters a thermal high separation tank, thermal high-pressure gas and thermal high-pressure oil are separated, and the separated thermal high-pressure gas is taken as the heat mediums to pass through the first heat medium channel of the first winding tube type heat exchanger and is output by the first winding tube type heat exchanger; and taking the low-oil in the second pipeline as a cooling medium to sequentially travel through a first cooling medium channel II of the first winding tube type heat exchanger and a third cooling medium channel of the third winding tube type heat exchanger, wherein the temperature of the low-oil in the second pipeline is 45-65 ℃, the pressure is less than 2.5MPa, and the temperature of the low-oil discharged from the third winding tube type heat exchanger is 170-215 ℃ and the low-oil is sent to downstream equipment I.
Compared with the prior art, the application has the advantages that: by designing the heat exchange device as a first wound tube heat exchanger with one first heat medium channel and at least two first cold medium channels, a second wound tube heat exchanger with one second heat medium channel and at least one second cold medium channel, a third wound tube heat exchanger with one third cold medium channel and at least one third heat medium channel, the number of heat exchangers can be reduced, and thus the equipment occupation, the frame investment, the high-pressure pipeline consumption, the piping work, the maintenance cost of the equipment and the like can be reduced; the first, second and third winding tube heat exchangers can be matched to realize and improve the heat exchange effect of the combined heat exchangers, 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 the prior art; meanwhile, the application can reduce the pressure drop of the whole device, and has obvious advantages; the application has simple structure and convenient implementation.
Drawings
FIG. 1 is a schematic diagram of a first embodiment of the present invention;
FIG. 2 is a schematic diagram of a second embodiment of the present invention;
Fig. 3 is a schematic structural view of a first coiled tube heat exchanger according to a third embodiment of the present invention;
Fig. 4 is a schematic structural view of a first coiled 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 embodiments of the drawings.
Embodiment one:
referring to fig. 1, a hydrogenation heat exchange system and a heat exchange process using a multi-stream wound tube heat exchanger according to a preferred embodiment of the present invention are shown, wherein the hydrogenation heat exchange system comprises 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 thermal high separation tank 8.
The first pipeline 1 is used for conveying a mixture composed 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 conveying low-split 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, and the thermal high-pressure oil output by the thermal high-pressure oil output end 82 can be subjected to the existing cold high-pressure tank and the cold low-pressure tank in sequence 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 a first heat medium passage 41 and two first cold medium passages, and the first wound tube heat exchanger 4a is provided with a first heat medium passage inlet connection pipe 411 and a first heat medium passage outlet connection pipe 412 which are communicated with the first heat medium passage 41, a first cold medium passage first inlet connection pipe 421 and a first cold medium passage first outlet connection pipe 422 which are communicated with the first cold medium passage first 42, a first cold medium passage second inlet connection pipe 471 and a first cold medium passage second outlet connection pipe 472 which are communicated with the first cold medium passage 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 passage inlet nipple 431 and a second heat medium passage outlet nipple 432 which communicate with the second heat medium passage 43, and a second cold medium passage inlet nipple 441 and a second cold medium passage outlet nipple 442 which communicate with the second cold medium passage 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 cooling medium passage inlet nipple 451 and a third cooling medium passage outlet nipple 452 which communicate with the third cooling medium passage 45, and a third heating medium passage inlet nipple 461 and a third heating medium passage outlet nipple 462 which communicate with the third heating 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 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.
The connection structure between each heat exchanger and each pipeline, heating furnace, hydrogenation reactor, thermal high separation tank in this embodiment is:
The first cold medium channel one inlet connecting pipe 421 of the first winding tube type heat exchanger 4a is connected with the output end of the first pipeline 1, the first cold medium channel one outlet connecting pipe 422 is connected with the second cold medium channel inlet connecting pipe 441 of the second winding tube type heat exchanger 4b, and the second cold medium channel outlet connecting pipe 442 is connected with the input end of the heating furnace 6; the second heat medium channel inlet connection pipe 431 is connected with the output end of the hydrogenation reactor 7, the second heat medium channel outlet connection pipe 432 is connected with the third heat medium channel inlet connection pipe 461 of the third winding pipe type heat exchanger 4c, the third heat medium channel outlet connection pipe 462 is connected with the input end of the heat high separation tank 8, the heat high-pressure gas output end 81 on the heat high separation tank 8 and the output end of the third pipeline 3 are connected with the first heat medium channel inlet connection pipe 411 in the first winding pipe type heat exchanger 4a after being connected, and the first heat medium channel outlet connection pipe 412 is connected to the second downstream equipment 9; the first second cold medium channel inlet connection 471 of the first wound tube heat exchanger 4a is connected to the output of the second pipeline 2, the first second outlet connection 472 of the first cold medium channel is connected to the third cold medium channel inlet connection 451 of the third wound tube heat exchanger 4c, and the third cold medium channel outlet connection 452 is connected to the first downstream device.
In this embodiment, the downstream device two 9 is a high-pressure air cooler, and the heat medium from the first heat medium channel outlet connection pipe 412 is connected to the cold high-air separation tank after passing through the high-pressure air cooler, so as to separate the 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 heat exchange method by adopting the hydrogenation heat exchange system of the embodiment is as follows:
The mixture of the raw oil and the hydrogen in the first pipeline 1 sequentially passes through one tube pass of the first winding tube heat exchanger 4a and the tube pass of the second winding tube heat exchanger 4b and then is output from the second winding tube heat exchanger 4b, the temperature of the raw oil and the hydrogen in the first pipeline 1 is 70 ℃, 83.4 ℃ respectively, and the temperature of the mixture output from the second winding tube heat exchanger 4b is 330-388 ℃; the mixture from the second winding tube heat exchanger 4b is output from the hydrogenation reactor 7 after passing through the heating furnace 6 and the hydrogenation reactor 7, the temperature of the output reaction product is 370-415 ℃, the reaction product sequentially goes through the shell side of the second winding tube heat exchanger 4b and the tube side of the third winding tube heat exchanger 3c as a heat medium, the temperature of the reaction product from the tube side of the third winding tube heat exchanger 3c is reduced to 230 ℃, then the reaction product enters the thermal high-pressure separation tank 8, the thermal high-pressure gas and the thermal high-pressure oil are separated, the separated thermal high-pressure gas and the water in the third pipeline 3 are mixed and then go through the shell side of the first winding tube heat exchanger 4a, the temperature of the thermal high-pressure gas and the water from the shell side of the first winding tube heat exchanger 4a is reduced to 105 ℃, and then the reaction product enters the second downstream equipment 9. The low-oil-content in the second pipeline 2 sequentially goes through the other tube side of the first winding tube type heat exchanger 4a and the shell side of the third winding tube type heat exchanger 4c, the temperature of the low-oil-content in the second pipeline 2 is 55 ℃, the temperature of the low-oil-content from the shell side of the third winding tube type heat exchanger 4c is 185-207 ℃, and the low-oil-content is sent to the first downstream equipment.
Embodiment two:
as shown in fig. 2, a hydrogenation heat exchange system and a heat exchange process using a multi-stream wound tube heat exchanger according to a preferred embodiment of the present invention are 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 in that 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 481 and a first cold medium channel three outlet connection 482 which are in communication with the 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 pipeline 30 for delivering water, the first cold medium channel three-inlet adapter 481 is connected to an output end of the fourth pipeline 30, and the first cold medium channel three-outlet adapter 482 is connected to a downstream apparatus three. In this way, 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 the hot water, in this embodiment, the hot water coming out of the first cold medium channel three outlet connecting pipe 482 can be conveyed into the third pipeline 3.
The heat exchange method by adopting the hydrogenation heat exchange system of the embodiment is as follows:
The mixture in the first pipeline 1 sequentially passes through one tube pass of the first winding tube heat exchanger 4a and the tube pass of the second winding tube heat exchanger 4b and then is output from the second winding tube heat exchanger 4b, the temperature of the mixture in the first pipeline 1 is 130 ℃, and the temperature of the mixture output from the second winding tube heat exchanger 4b is 330-388 ℃; the mixture from the second winding tube heat exchanger 4b is output from the hydrogenation reactor 7 after passing through the heating furnace 6 and the hydrogenation reactor 7, the temperature of the output reaction product is 370-415 ℃, the reaction product sequentially goes through the shell side of the second winding tube heat exchanger 4b and the tube side of the third winding tube heat exchanger 3c as a heat medium, the temperature of the reaction product from the tube side of the third winding tube heat exchanger 3c is reduced to 230 ℃, then the reaction product enters the thermal high-pressure separation tank 8, the thermal high-pressure gas and the thermal high-pressure oil are separated, the separated thermal high-pressure gas and the water in the third pipeline 3 are mixed and then go through the shell side of the first winding tube heat exchanger 4a, the temperature of the thermal high-pressure gas and the water from the shell side of the first winding tube heat exchanger 4a is reduced to 95 ℃, and then the reaction product enters the second downstream equipment 9. The low-oil-content in the second pipeline 2 sequentially goes through the other tube side of the first winding tube type heat exchanger 4a and the shell side of the third winding tube type heat exchanger 4c, the temperature of the low-oil-content in the second pipeline 2 is 55 ℃, the temperature of the low-oil-content from the shell side of the third winding tube type heat exchanger 4c is 185-207 ℃, and the low-oil-content 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 exiting the first wound tube heat exchanger 4a is 95 ℃, and sent to the downstream apparatus three.
Embodiment III:
As shown in fig. 3, a third preferred embodiment of the present invention of a hydrogenation heat exchange system and heat exchange process using a multi-stream wound tube heat exchanger is basically the same as the first preferred embodiment, except that the first wound tube heat exchanger 4a in this preferred embodiment is slightly different from the first wound tube heat exchanger in the first preferred embodiment, the first heat medium channel 41 in this preferred embodiment 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.
Embodiment four:
as shown in fig. 4, a fourth preferred embodiment of the present invention of a hydrogenation heat exchange system and heat exchange process using a multi-stream wound tube heat exchanger is basically the same as the second embodiment, except that the first wound tube heat exchanger 4a in this embodiment is slightly different from the first wound tube heat exchanger in the second embodiment, the first heat medium channel 41 in this embodiment 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.
Fifth embodiment:
As shown in fig. 5, a fifth preferred embodiment of the present invention is a heat exchange system and heat exchange process using a multi-stream wound tube heat exchanger, which is substantially the same as the first embodiment except that the second downstream apparatus 9 in this embodiment is a wound tube heat exchanger having a heat medium passage 92 and a cold medium passage 91. The hydrogenation heat exchange system of the embodiment further comprises a cold water pipeline 100 for conveying cold water, wherein the output end of the cold water pipeline 100 is connected with an inlet connecting pipe of a cold medium channel 91 of a second downstream device 9, the inlet connecting pipe of a heat medium channel 92 of the second downstream device 9 is connected with a first heat medium channel outlet connecting pipe 412 of the first winding tube type heat exchanger 4a, and the outlet connecting pipe of the heat medium channel 92 is connected to a cold high separation tank 93.
Meanwhile, the hydrogenation heat exchange system of this 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 cold medium channel outlet connection pipe 442 of the second winding pipe heat exchanger 4b, the first valve 120 is disposed on the bypass line 110, and the second valve 130 is disposed 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 with the second pipeline 2, and the output end of the fifth pipeline 140 is connected with a third cold medium channel outlet connecting pipe 452 of the third winding pipe type heat exchanger 4 c; 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 second line 2. The input end of the sixth pipeline 170 is connected with the first pipeline 1, and the output end is connected between the input end of the heating furnace 6 and the second cold medium channel outlet connection pipe 442 of the second winding tube type heat exchanger 4 b; the fifth valve 180 is disposed on the sixth line 170, and the sixth valve 190 is disposed between the output of the first line 1 and the input of the sixth line 170. The bypass line 110, the fifth line 140, the sixth line 170 and the valves are arranged to satisfy the process conditions of each stage and each working condition variation of the device. The on-off of each pipeline is selected according to the actual working condition.
The hydrogenation heat exchange system of the embodiment is adopted for heat exchange, and comprises the following steps:
the mixture of raw oil and hydrogen in the first pipeline 1 is taken as a cooling medium to be sequentially output from the second winding tube heat exchanger 4b after passing through a first cooling medium channel 42 of the first winding tube heat exchanger 4a and a second cooling medium channel 44 of the second winding tube 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 discharged from the second winding tube heat exchanger 4b is 330-388 ℃; the mixture from the second winding tube heat exchanger 4b enters the hydrogenation reactor 7 to carry out hydrogenation reaction, then the mixture is output from the hydrogenation reactor 7, the temperature of the output reaction product is 370-415 ℃, the reaction product sequentially goes through the second heat medium channel 43 of the second winding tube heat exchanger 4b and the third heat medium channel 46 of the third winding tube heat exchanger 4c as heat medium, the temperature of the reaction product from the third winding tube heat exchanger 4c is reduced to 230 ℃, then the reaction product enters the high-temperature separation tank 8 to separate high-temperature gas and high-temperature oil, the separated high-temperature gas is taken as heat medium to pass through the first heat medium channel 41 of the first winding tube heat exchanger 4a, the temperature of the output medium is 105 ℃, then enters the heat medium channel 92 of the second downstream equipment 9, the temperature of cold water (the water temperature is lower than 35 ℃) in the cold line 100 is lower than 45 ℃, the temperature of the water coming out from the cold medium channel 91 of the second downstream equipment 9 is lower than 45 ℃, and the separated high-temperature gas is sent into the high-temperature separation tank 50 through the first heat medium channel 41 of the first winding tube heat exchanger 4a, the output medium is sent into the high-temperature medium channel 92 of the second equipment 9; meanwhile, the low-oil in the second pipeline 2 is taken as a cooling medium to sequentially travel through a second cooling medium channel 47 of the first winding tube type heat exchanger 4a and a third cooling medium channel 45 of the third winding tube type heat exchanger 4c, the temperature of the low-oil in the second pipeline 2 is 55 ℃, the pressure is less than 2.5MPa, the temperature of the low-oil discharged from the third winding tube type heat exchanger 4c is 185-207 ℃, and the low-oil is sent to a first downstream device.
The hydrogenation heat exchange system of this embodiment has high heat exchange efficiency, so that the mixture coming out of the second winding tube heat exchanger 4b can directly enter the hydrogenation reactor 7 for reaction without heating by a heating furnace, the heating furnace only needs to be used at the initial stage of operation, and the bypass pipeline 110 can be used at other operation stages.
Example six:
The technical scheme of the embodiment is basically the same as that of the first embodiment, and the difference is that the heat exchange process is slightly different, and the method for carrying out heat exchange by adopting the hydrogenation heat exchange system of the embodiment is as follows:
The mixture consisting of raw oil and hydrogen in the first pipeline 1 sequentially passes through one tube pass of the first winding tube heat exchanger 4a and the tube pass of the second winding tube heat exchanger 4b and then is output from the second winding tube 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 by the second winding tube heat exchanger 4b is 320 ℃; the mixture from the second winding tube heat exchanger 4b is output from the hydrogenation reactor 7 after passing through the heating furnace 6 and the hydrogenation reactor 7, the temperature of the output reaction product is 355 ℃, the reaction product sequentially goes through the shell side of the second winding tube heat exchanger 4b and the tube side of the third winding tube heat exchanger 3c as a heat medium, the temperature of the reaction product from the tube side of the third winding tube heat exchanger 3c is reduced to 220 ℃, then the reaction product enters the thermal high-separation tank 8, the thermal high-pressure gas and the thermal high-pressure oil are separated, the separated thermal high-pressure gas and the water in the third pipeline 3 are mixed and then go through the shell side of the first winding tube heat exchanger 4a, the temperature of the thermal high-pressure gas and the water from the shell side of the first winding tube heat exchanger 4a is reduced to 105 ℃, and then the reaction product enters the second downstream equipment 9. The low-oil in the second pipeline 2 sequentially goes through the other tube side of the first winding tube type heat exchanger 4a and the shell side of the third winding tube type heat exchanger 4c, the temperature of the low-oil in the second pipeline 2 is 45 ℃, the pressure is 2.0MPa, and the temperature of the low-oil discharged from the shell side of the third winding tube type heat exchanger 4c is 170 ℃ and is sent to the downstream equipment I.
Embodiment seven:
The technical scheme of the embodiment is basically the same as that of the first embodiment, and the difference is that the heat exchange process is slightly different, and the method for carrying out heat exchange by adopting the hydrogenation heat exchange system of the embodiment is as follows:
Sequentially passing a mixture consisting of raw oil and hydrogen in a first pipeline 1 through one tube pass of a first winding tube heat exchanger 4a and one tube pass of a second winding tube heat exchanger 4b, and then outputting the mixture from the second winding tube heat exchanger 4b, wherein the temperature of the mixture in the first pipeline 1 is 165 ℃, the pressure is 19MPa, and the temperature of the mixture discharged from the second winding tube heat exchanger 4b is 395 ℃; the mixture from the second winding tube heat exchanger 4b is output from the hydrogenation reactor 7 after passing through the heating furnace 6 and the hydrogenation reactor 7, the temperature of the output reaction product is 420 ℃, the reaction product sequentially goes through the shell side of the second winding tube heat exchanger 4b and the tube side of the third winding tube heat exchanger 3c as a heat medium, the temperature of the reaction product from the tube side of the third winding tube heat exchanger 3c is reduced to 260 ℃, then the reaction product enters the thermal high-pressure separation tank 8, the thermal high-pressure gas and the thermal high-pressure oil are separated, the separated thermal high-pressure gas and the water in the third pipeline 3 are mixed and then go through the shell side of the first winding tube heat exchanger 4a, the temperature of the thermal high-pressure gas and the water from the shell side of the first winding tube heat exchanger 4a is reduced to 105 ℃, and then the reaction product enters the second downstream equipment 9. The low-oil in the second pipeline 2 sequentially goes through the other tube side of the first winding tube type heat exchanger 4a and the shell side of the third winding tube type heat exchanger 4c, the temperature of the low-oil in the second pipeline 2 is 65 ℃, the pressure is 1.5MPa, and the temperature of the low-oil discharged from the shell side of the third winding tube type heat exchanger 4c is 215 ℃ and is sent to the downstream equipment I.
The temperatures of the raw oil, the hydrogen and the low-pressure oil in the embodiments can be different according to actual working conditions, and the data are shown only for showing that after the heat exchange device in the embodiments is adopted, compared with the heat exchange device in the existing hydrogenation process, the heat exchange effect is good, so that the number of heat exchangers can be reduced, the equipment occupation, the equipment investment, the high-pressure pipeline consumption, the piping work, the equipment maintenance cost and the like can be reduced, the pressure drop of the whole device can be reduced, and the whole device is simple in structure and convenient to implement.
Claims (10)
1. A hydro-heat exchange system employing a multi-stream wound tube heat exchanger, comprising: a first pipeline (1) for conveying a mixture composed of raw oil and hydrogen, a second pipeline (2) for conveying low-pressure oil, a heating furnace (6), a hydrogenation reactor (7) connected with the output end of the heating furnace (6), a thermal high separation tank (8) for separating reaction products output by the hydrogenation reactor (7) to obtain thermal high-pressure gas and thermal high-pressure oil, and a heat exchange device (4), wherein the thermal high-pressure gas and the thermal high-pressure oil are characterized in that:
The heat exchange device (4) comprises a first wound tube heat exchanger (4 a) with one first heat medium channel (41) and at least two first cold medium channels, a second wound tube heat exchanger (4 b) with one second heat medium channel (43) and at least one second cold medium channel (44), a third wound tube heat exchanger (4 c) with one third cold medium channel (45) and at least one third heat medium channel (46);
The first winding tube type heat exchanger (4 a) 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), 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); the second winding tube type heat exchanger (4 b) is provided with a second heat medium channel inlet connecting tube (431) and a second heat medium channel outlet connecting tube (432) which are communicated with a second heat medium channel (43), and a second cold medium channel inlet connecting tube (441) and a second cold medium channel outlet connecting tube (442) which are communicated with a second cold medium channel (44); 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 winding pipe type heat exchanger (4 c);
the first cold medium channel one inlet connecting pipe (421) of the first winding pipe type heat exchanger (4 a) is connected with the output end of the first pipeline (1), the first cold medium channel one outlet connecting pipe (422) is connected with the second cold medium channel inlet connecting pipe (441) of the second winding pipe type heat exchanger (4 b), and the second cold medium channel outlet connecting pipe (442) 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 winding pipe type heat exchanger (4 c), the third heat medium channel outlet connecting pipe (462) is connected with the input end of the heat high separation tank (8), a heat high-pressure gas output end (81) for outputting heat high-pressure gas on the heat high separation tank (8) is connected with a first heat medium channel inlet connecting pipe (411) in the first winding pipe type heat exchanger (4 a), and the first heat medium channel outlet connecting pipe (412) is connected to a downstream equipment II (9); a second inlet connection pipe (471) of the first cold medium channel of the first winding tube type heat exchanger (4 a) is connected with the output end of the second pipeline (2), a second outlet connection pipe (472) of the first cold medium channel is connected with a third cold medium channel inlet connection pipe (451) of the third winding tube type heat exchanger (4 c), and a third cold medium channel outlet connection pipe (452) is connected to a first downstream device;
The second heat medium channel (43) is a shell side of the second winding tube heat exchanger (4 b), the second cooling medium channel (44) is a tube side of the second winding tube heat exchanger (4 b), and the second winding tube heat exchanger (4 b) is a single-flow winding tube heat exchanger with one shell side and one tube side;
the third heat medium channel (46) is a tube side of the third winding tube heat exchanger (4 c), the third cooling medium channel (45) is a shell side of the third winding tube heat exchanger (4 c), and the third winding tube heat exchanger (4 c) is a single-flow winding tube heat exchanger with one shell side and one tube side.
2. The hydro-heat exchange system according to claim 1, wherein: the heat exchanger further comprises a fourth pipeline (30) for conveying water, at least three first cold medium channels are arranged in the first winding tube type heat exchanger (4 a), and the first winding tube type heat exchanger (4 a) is further provided with 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); the first cold medium channel three-inlet connecting pipe (481) is connected with the output end of the fourth pipeline (30), and the first cold medium channel three-outlet connecting pipe (482) is connected to a downstream device three.
3. The hydro-heat exchange system according to claim 1, wherein: the first heat medium channel (41) is a shell side of the first winding tube heat exchanger (4 a), the first cooling medium channel is a tube side of the first winding tube heat exchanger (4 a), and the first winding tube heat exchanger (4 a) is a double-flow winding tube heat exchanger with one shell side and two tube sides.
4. The hydro-heat exchange system according to claim 2, wherein: the first heat medium channel (41) is a shell side of the first winding tube heat exchanger (4 a), the first cooling medium channel is a tube side of the first winding tube heat exchanger (4 a), and the first winding tube heat exchanger (4 a) is a three-stream winding tube heat exchanger with one shell side and three tube sides.
5. The hydro-heat exchange system according to any one of claims 1-4, wherein: the high-temperature separator is characterized by further comprising a third pipeline (3) for conveying water, wherein a high-temperature gas output end (81) of the high-temperature separator tank (8) for outputting high-temperature gas is connected with the output end of the third pipeline (3) and then connected with the first winding tube type heat exchanger (4 a).
6. The hydro-heat exchange system according to any one of claims 1-4, wherein: the downstream equipment II (9) is a high-pressure air cooler;
Or, the second downstream device (9) is a coiled tube heat exchanger with one 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 an inlet connecting tube of the cold medium channel (91) of the second downstream device (9), an inlet connecting tube of the heat medium channel (92) of the second downstream device (9) is connected with a first heat medium channel outlet connecting tube (412) of the first coiled tube heat exchanger (4 a), and an outlet connecting tube of the heat medium channel (92) is connected to a cold high separation tank (93).
7. The hydro-heat exchange system according to any one of claims 1-4, 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 a second cold medium channel outlet connecting pipe (442) of the second winding pipe type heat exchanger (4 b), 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).
8. The hydro-heat exchange system according to any one of claims 1-4, wherein: the device 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 winding pipe 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).
9. The hydro-heat exchange system according to any one of claims 1-4, wherein: the heating furnace further 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 winding pipe type heat exchanger (4 b); the fifth valve (180) is arranged on the 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).
10. A heat exchange process for heat exchange by using the hydrogenation heat exchange system according to any one of claims 1 to 9, characterized by comprising the steps of:
The mixture of raw oil and hydrogen in a first pipeline (1) is taken as a cold medium to sequentially pass through a first cold medium channel I (42) of a first winding tube type heat exchanger (4 a) and a second cold medium channel (44) of a second winding tube type heat exchanger (4 b) and then output from the second winding tube type heat exchanger (4 b), 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 discharged from the second winding tube type heat exchanger (4 b) is 320-395 ℃; the mixture coming out of the second winding tube type heat exchanger (4 b) enters a hydrogenation reactor (7) for hydrogenation reaction, then is output from the hydrogenation reactor (7), the temperature of the output reaction product is 355-420 ℃, the reaction product sequentially goes through a second heat medium channel (43) of the second winding tube type heat exchanger (4 b) and a third heat medium channel (46) of the third winding tube type heat exchanger (4 c) as heat mediums, the temperature of the reaction product coming out of the third winding tube type heat exchanger (4 c) is reduced to 220-260 ℃, then enters a thermal high separation tank (8), and the thermal high-pressure gas and the thermal high-pressure oil are separated, and the separated thermal high-pressure gas is taken as the heat mediums to pass through a first heat medium channel (41) of the first winding tube type heat exchanger (4 a) and is output by the first winding tube type heat exchanger (4 a); and taking the low-oil in the second pipeline (2) as a cooling medium to sequentially travel through a first cooling medium channel II (47) of the first winding tube type heat exchanger (4 a) and a third cooling medium channel (45) of the third winding tube type heat exchanger (4 c), wherein the temperature of the low-oil in the second pipeline (2) is 45-65 ℃, the pressure is less than 2.5 MPa, and the low-oil temperature discharged by the third winding tube type heat exchanger (4 c) is 170-215 ℃ and is sent to downstream equipment I.
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| CN113532156B (en) * | 2021-08-11 | 2024-06-04 | 镇海石化建安工程股份有限公司 | Atmospheric and vacuum heat exchange system with winding tube type heat exchanger |
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| CN210700039U (en) * | 2019-08-23 | 2020-06-09 | 镇海石化建安工程有限公司 | Depolymerization system with winding tube heat exchanger |
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