CN215572361U - Hydrogenation heat exchange system adopting multi-strand winding tube type heat exchanger - Google Patents

Abstract

A hydroprocessing heat exchange system, comprising: the device comprises a first pipeline (1), a second pipeline (2), a heating furnace (6), a hydrogenation reactor (7), a heat high separation tank (8) and a heat exchange device, wherein the heat exchange device comprises a first heat exchange device (4) for performing primary heat exchange on heat high-pressure gas and a mixture in the first pipeline (1) and low-pressure oil in the second pipeline (2), and a second heat exchange device (5) which is connected with a mixture output end and a low-pressure oil output end at the tail end of the first heat exchange device and is used for performing secondary heat exchange on the mixture after the primary heat exchange and the low-pressure oil; the second heat exchange device (5) is a second wound tube heat exchanger with one second heat medium channel (51) and at least two second cold medium channels. 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

Hydrogenation heat exchange system adopting multi-strand winding tube type heat exchanger

Technical Field

The utility model belongs to the technical field of heat exchange, and particularly relates to a hydrogenation heat exchange system 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 utility model 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.

SUMMERY OF THE UTILITY MODEL

The utility model aims to solve the technical problem of providing 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 technical scheme adopted by the utility model for solving the technical problems 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 heat exchange device and a second heat exchange device, the first heat exchange device is connected with a high-temperature gas separation output end of the first pipeline, the second pipeline and the high-temperature separation tank, which is used for outputting high-temperature gas, and is used for carrying out primary heat exchange on the high-temperature gas separation, the mixture in the first pipeline and the low-temperature oil in the second pipeline; the second heat exchange device is connected with the mixture output end and the low oil separation output end of the first heat exchange device and is used for carrying out secondary heat exchange on the mixture and the low oil separation after primary heat exchange;

the second heat exchange device is a second wound tube type heat exchanger with a second heat medium channel and at least two second cold medium channels, and the second wound tube type heat exchanger is provided with a second heat medium channel inlet connecting tube and a second heat medium channel outlet connecting tube which are communicated with the second heat medium channel, a second cold medium channel first inlet connecting tube and a second cold medium channel first outlet connecting tube which are communicated with the second cold medium channel first, a second cold medium channel second inlet connecting tube and a second cold medium channel second outlet connecting tube which are communicated with the second cold medium channel second;

the inlet connecting pipe of the second heat medium channel is connected with the output end of the hydrogenation reactor, the outlet connecting pipe of the second heat medium channel is connected with the input end of the high-temperature separation tank, the inlet connecting pipe of the first cold medium channel is connected with the mixture output end at the tail end of the first heat exchange device, the outlet connecting pipe of the first cold medium channel is connected with the input end of the heating furnace, the inlet connecting pipe of the second cold medium channel is connected with the low oil output end at the tail end of the first heat exchange device, and the outlet connecting pipe of the second cold medium channel is connected to the first downstream equipment.

Preferably, the first heat exchange device is a first wound tube heat exchanger with one first heat medium channel and at least two first cold medium channels, the first wound tube heat exchanger is provided with a first heat medium channel inlet connecting pipe and a first heat medium channel outlet connecting pipe which are communicated with the first heat medium channel, a first cold medium channel first inlet connecting pipe and a first cold medium channel first outlet connecting pipe which are communicated with the first cold medium channel first, and a first cold medium channel second inlet connecting pipe and a first cold medium channel second outlet connecting pipe which are communicated with the first cold medium channel second;

the inlet connecting pipe of the first heat medium channel is connected with a heat high-pressure gas output end of the heat high-pressure separation tank, which is used for outputting heat high-pressure gas, the outlet connecting pipe of the first heat medium channel is connected to a second downstream device, the first inlet connecting pipe of the first cold medium channel is connected with the output end of the first pipeline, and the second inlet connecting pipe of the first cold medium channel is connected with the output end of the second pipeline;

and the first outlet connecting pipe of the first cold medium channel and the second outlet connecting pipe of the first cold medium channel are respectively a mixture output end and a low oil separation output end at the tail end of the first heat exchange device.

In the above scheme, the heat exchanger further comprises a fourth pipeline for conveying water, the number of the first cold medium channels in the first heat exchanger is at least three, and the first heat exchanger is further provided with a third inlet connecting pipe of the first cold medium channel and a third outlet connecting pipe of the first cold medium channel, which are communicated with the third cold medium channel; the third inlet connecting pipe of the first cold medium channel is connected with the output end of the fourth pipeline, and the third outlet connecting pipe of the first cold medium channel is connected to a third downstream device;

or, the heat exchanger further comprises a fourth pipeline for conveying water and a fifth wound tube heat exchanger, the fifth wound tube heat exchanger is provided with a fifth heat medium channel and at least one fifth cold medium channel, the fifth wound tube heat exchanger is provided with a fifth cold medium channel inlet connecting pipe and a fifth cold medium channel outlet connecting pipe which are communicated with the fifth cold medium channel, the fifth cold medium channel inlet connecting pipe is connected with the output end of the fourth pipeline, the fifth cold medium channel outlet connecting pipe is connected to a third downstream device, and the first heat medium channel outlet connecting pipe in the first heat exchange device is connected to the second downstream device through the fifth heat medium channel.

Also preferably, the first heat exchange device comprises a third wound tube heat exchanger with a third heat medium channel and at least one third cold medium channel, and a fourth wound tube heat exchanger with a fourth heat medium channel and at least one fourth cold medium channel, the third wound tube heat exchanger is provided with a third heat medium channel inlet connecting tube and a third heat medium channel outlet connecting tube which are communicated with the third heat medium channel, a third cold medium channel inlet connecting tube and a third cold medium channel outlet connecting tube which are communicated with the third cold medium channel, the fourth wound tube heat exchanger is provided with a fourth heat medium channel inlet connecting tube and a fourth heat medium channel outlet connecting tube which are communicated with the fourth heat medium channel, a fourth cold medium channel inlet connecting tube and a fourth cold medium channel outlet connecting tube which are communicated with the fourth cold medium channel;

the third cold medium channel inlet connecting pipe is connected with the output end of the first pipeline, the third hot medium channel inlet connecting pipe is connected with a hot high-pressure gas distribution output end of the hot high-pressure separation tank, which is used for outputting hot high-pressure gas, the third hot medium channel outlet connecting pipe is connected with the fourth hot medium channel inlet connecting pipe, the fourth hot medium channel outlet connecting pipe is connected to a second downstream device, and the fourth cold medium channel inlet connecting pipe is connected with the output end of the second pipeline;

and the outlet connecting pipe of the third cold medium channel and the outlet connecting pipe of the fourth cold medium channel are respectively a mixture output end and a low oil separation output end at the tail end of the first heat exchange device.

The fifth wound tube type heat exchanger is provided with a fifth cold medium channel inlet connecting pipe and a fifth cold medium channel outlet connecting pipe which are communicated with the fifth cold medium channel, the fifth cold medium channel inlet connecting pipe is connected with the output end of the fourth pipeline, the fifth cold medium channel outlet connecting pipe is connected to a third downstream device, and the fourth hot medium channel outlet connecting pipe in the fourth wound tube type heat exchanger is connected to a second downstream device through the fifth hot medium channel.

In each of the above aspects, preferably, the second heat medium channel is a shell side of the second wound tube heat exchanger, the second cold medium channel is a tube side of the second wound tube heat exchanger, and the second heat exchange device is a double-flow wound tube heat exchanger having one shell side and two tube sides. As an alternative, the second heat medium channel may also be a tube side of the second wound tube heat exchanger, the second cold medium channel is a shell side of the second wound tube heat exchanger, and the second heat exchange device is a wound tube heat exchanger having two shell sides and one tube side.

Preferably, the first heat medium channel is a shell side of the first wound tube heat exchanger, the first cold medium channel is a tube side of the first wound tube heat exchanger, and the first heat exchange device is a double-stream wound tube heat exchanger having one shell side and two tube sides. As an alternative, the first heat medium channel may also be a tube side of the first wound tube heat exchanger, the first cold medium channel is a shell side of the first wound tube heat exchanger, and the first heat exchanging device is a wound tube heat exchanger having one tube side and two shell sides.

Preferably, the third heat medium channel is a tube side of the third wound tube heat exchanger, the third cold medium channel is a shell side of the third wound tube heat exchanger, and the third wound tube heat exchanger is a single-flow wound tube heat exchanger having one shell side and one tube side. Alternatively, the third heat medium channel may be a shell side of the third wound tube heat exchanger, and the third cold medium channel may be a tube side of the third wound tube heat exchanger.

Preferably, the fourth heat medium channel is a tube side of the fourth wound tube heat exchanger, the fourth cold medium channel is a shell side of the fourth wound tube heat exchanger, and the fourth wound tube heat exchanger is a single-flow wound tube heat exchanger having one shell side and one tube side. Alternatively, the fourth heat medium channel may be a shell side of the fourth wound tube heat exchanger, and the fourth cold medium channel may be a tube side of the fourth wound tube heat exchanger.

Preferably, the fifth heat medium channel is a tube side of the fifth wound tube heat exchanger, the fifth cold medium channel is a shell side of the fifth wound tube heat exchanger, and the fifth wound tube heat exchanger is a single-flow wound tube heat exchanger having one shell side and one tube side. Alternatively, the fifth heat medium channel may also be a shell side of the fifth wound tube heat exchanger, and the fifth cooling medium channel is a tube side of the fifth wound tube heat exchanger.

In each scheme, the heat recovery system further comprises a third pipeline for conveying water, and a heat high-pressure gas output end of the heat high-pressure separation tank for outputting heat high-pressure gas is connected with an output end of the third pipeline and then connected with the first heat exchange device. Therefore, water can dissolve part of media such as hydrogen sulfide and ammonium salt in the hot high-pressure gas so as to reduce the phenomenon that part of media in the hot high-pressure gas corrodes the heat exchanger.

Preferably, the second downstream equipment is a high-pressure air cooler;

or the downstream equipment II is a wound tube heat exchanger with a hot medium channel and at least one cold medium channel, and further comprises a cold water pipeline for conveying cold water, the output end of the cold water pipeline is connected with the inlet connecting pipe of the cold medium channel of the downstream equipment II, the inlet connecting pipe of the hot medium channel of the downstream equipment II is connected with the output end of the first heat exchange device for outputting heat-exchanged hot high-pressure gas, and the outlet connecting pipe of the hot medium channel is connected to the cold high separation tank.

Namely, a wound tube type heat exchanger can be used for replacing a high-pressure air cooler, a hydrogenation device usually needs a plurality of high-pressure air coolers, and each air cooler is about 10.5 x 3m in size, large in volume and large in occupied area; and one vertically-installed winding tube type heat exchanger can meet the process requirements, so that the occupied area is greatly reduced.

In each of the above schemes, preferably, the system further includes a bypass line, a first valve and a second valve, an output end of the bypass line is connected between an output end of the heating furnace and an input end of the hydrogenation reactor, an input end of the bypass line is connected between an input end of the heating furnace and an outlet connection pipe of a second cold medium channel of the second heat exchange device, the first valve is disposed on the bypass line, and the second valve is disposed between the input end of the heating furnace and the input end of the bypass line. That is, the heating furnace in the present application is a start-up heating furnace, and only needs to perform heating operation in a start-up stage (i.e., the initial stage of system operation), and the rest stages do not need to operate. The heat exchange device can achieve better heat exchange effect, greatly reduce the operation load of the heating furnace, and can achieve the purpose by adopting the heating furnace with smaller volume and smaller heating capacity.

Preferably, the heat exchanger further comprises a fifth pipeline, a third valve and a fourth valve, wherein the input end of the fifth pipeline is connected with the second pipeline, and the output end of the fifth pipeline is connected with a second outlet connecting pipe of a second cold medium channel of the second heat exchanger; the third valve is arranged on 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 an outlet connecting pipe of a second cold medium channel of the second heat exchange device; 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.

Compared with the prior art, the utility model has the advantages that: the heat exchange device is designed to comprise a first heat exchange device for performing primary heat exchange on the mixture and the low-fraction oil, and a second heat exchange device for performing secondary heat exchange on the mixture and the low-fraction oil after the primary heat exchange, and the second heat exchange device is a second wound tube type heat exchanger with a second heat medium channel and at least two second cold medium channels, so that the number of the heat exchangers can be reduced, and further the occupied area of equipment, the investment of a frame, the using amount of high-pressure pipelines, the work of pipe distribution, the maintenance cost of the equipment and the like are reduced; in addition, the first heat exchange device and the second heat exchange device can be matched to realize and improve the heat exchange effect after the combination of a plurality of heat exchangers in the prior art, hydrogenation reaction can be carried out without a heating furnace after the operation is stable, and the temperature difference of the hot end and the pressure drop of a medium are small; the bypass adjusting means of the heat exchange device is consistent with that of the prior art; meanwhile, the pressure drop of the whole device can be reduced, and the advantages are obvious; and the structure is simple and convenient to implement.

Drawings

FIG. 1 is a schematic structural diagram according to a first embodiment of the present invention;

FIG. 2 is a schematic structural diagram according to a second embodiment of the present invention;

FIG. 3 is a schematic structural diagram of a third embodiment of the present invention;

FIG. 4 is a schematic structural diagram of a fourth embodiment of the present invention;

FIG. 5 is a schematic structural diagram of a fifth embodiment of the present invention;

FIG. 6 is a schematic structural diagram of a first heat exchange device in a sixth embodiment of the present invention;

FIG. 7 is a schematic structural diagram of a first heat exchange device in a seventh embodiment of the present invention;

fig. 8 is a schematic structural diagram of an eighth embodiment of the present invention.

Detailed Description

The utility model 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 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 heat exchange device 4, a second heat exchange device 5, 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 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 heat exchange device 4 is a first wound tube heat exchanger having one first heat medium channel 41 and two first cold medium channels, and the first wound tube heat exchanger is provided with a first heat medium channel inlet connecting pipe 411 and a first heat medium channel outlet connecting pipe 412 which are communicated with the first heat medium channel 41, a first cold medium channel first inlet connecting pipe 421 and a first cold medium channel first outlet connecting pipe 422 which are communicated with the first cold medium channel first 42, and a first cold medium channel second inlet connecting pipe 431 and a first cold medium channel second outlet connecting pipe 432 which are communicated with the first cold medium channel second 43; in this embodiment, the first heat medium channel 41 is a shell side of the first wound tube heat exchanger, the first cold medium channel is a tube side of the first wound tube heat exchanger, and the first heat exchanging device 4 is a double-flow wound tube heat exchanger having one shell side and two tube sides.

The second heat exchange device 5 is a second wound tube heat exchanger having one second heat medium channel 51 and two second cold medium channels, and the second wound tube heat exchanger is provided with a second heat medium channel inlet connecting pipe 511 and a second heat medium channel outlet connecting pipe 512 which are communicated with the second heat medium channel 51, a second cold medium channel first inlet connecting pipe 521 and a second cold medium channel first outlet connecting pipe 522 which are communicated with the second cold medium channel first 52, and a second cold medium channel second inlet connecting pipe 531 and a second cold medium channel second outlet connecting pipe 532 which are communicated with the second cold medium channel second 53; the second heat medium channel 51 and the second cold medium channel are the tube side and the shell side of the second wound tube heat exchanger; in this embodiment, the second heat medium channel 51 is a shell pass of the second wound tube heat exchanger, the second cold medium channel is a tube pass of the second wound tube heat exchanger, and the second heat exchanging device 5 is a double-flow wound tube heat exchanger having one shell pass and two tube passes.

The connection structure between the first heat exchange device 4 and the second heat exchange device 5 and the pipelines, the heating furnace 6, the hydrogenation reactor 7 and the thermal high separation tank 8 is as follows: the hot high-pressure gas output end 81 is connected with the output end of the third pipeline 3 and then connected with the first heat medium channel inlet connecting pipe 411 in the first heat exchanging device 4, the first heat medium channel outlet connecting pipe 412 is connected with the second downstream equipment 9, the first cold medium channel first inlet connecting pipe 421 is connected with the output end of the first pipeline 1, the first cold medium channel first outlet connecting pipe 422 is connected with the second cold medium channel first inlet connecting pipe 521 in the second heat exchanging device 5, the first cold medium channel second inlet connecting pipe 431 is connected with the output end of the second pipeline 2, and the first cold medium channel second outlet connecting pipe 432 is connected with the second cold medium channel second inlet connecting pipe 531 in the second heat exchanging device 5. In the second heat exchange device 5, a second heat medium channel inlet connection pipe 511 is connected to the output end of the hydrogenation reactor 7, a second heat medium channel outlet connection pipe 512 is connected to the input end of the thermal high separation tank 8, a second first cold medium channel outlet connection pipe 522 is connected to the input end of the heating furnace 6, and a second cold medium channel outlet connection pipe 532 is connected to a 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 separation tank to separate 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 mixture composed of raw oil and hydrogen in the first pipeline 1 and the low oil in the second pipeline 2 are sequentially input into the corresponding tube passes of the first heat exchange device 4 and the second heat exchange device 5, the temperatures of the raw oil and the hydrogen in the first pipeline 1 are respectively 70 ℃ and 83.4 ℃, the temperature of the low oil in the second pipeline 2 is 55 ℃, and the temperatures of the mixture and the low oil from the second heat exchange device 5 are respectively 330-388 ℃ and 185-207 ℃. The mixture from the second heat exchange device 5 passes through the heating furnace 6 and the 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 taken as a heat medium of the second heat exchange device 5 to go through the shell pass of the second heat exchange device 5 and exchange heat with the medium in the tube pass of the second heat exchange device 5, the temperature of the reaction product from the second heat exchange device 5 is reduced to 230 ℃, the reaction product enters the thermal high separation tank 8 to separate thermal high-pressure gas and thermal high-pressure oil, the separated thermal high-pressure gas is mixed with water in the third pipeline 3 and then goes through the shell pass of the first heat exchange device 4 as a heat medium of the first heat exchange device 4 and exchanges heat with the medium in the tube pass of the first heat exchange device 4, and the temperature of the thermal high-pressure gas and the water from the first heat exchange device 4 is reduced to 105 ℃, and then the temperature of the thermal high-pressure gas and the water enters the second downstream equipment 9.

Example two:

as shown in fig. 2, in a second preferred embodiment of a hydrogenation heat exchange system using a multi-stream wound tube heat exchanger according to the present invention, this embodiment is substantially the same as the first embodiment, except that the first heat exchange device 4 in this embodiment is different from the first embodiment, the first heat exchange device 4 in this embodiment includes a third wound tube heat exchanger 4a having a third heat medium channel 45 and a third cold medium channel 46, and a fourth wound tube heat exchanger 4b having a fourth heat medium channel 47 and a fourth cold medium channel 48, the third wound tube heat exchanger 4a is provided with a third heat medium channel inlet connection pipe 451 and a third heat medium channel outlet connection pipe 452 communicating with the third heat medium channel 45, a third cold medium channel inlet connection pipe 461 and a third cold medium channel outlet connection pipe 462 communicating with the third cold medium channel 46, and the fourth wound tube heat exchanger 4b is provided with a fourth heat medium channel inlet connection pipe communicating with the fourth heat medium channel 47 A connection 471 and a fourth heat medium channel outlet connection 472, a fourth cold medium channel inlet connection 481 connecting the fourth cold medium channel 48 and a fourth cold medium channel outlet connection 482. In this embodiment, the third heat medium channel 45 is a tube side of the third wound tube heat exchanger 4a, the third cooling medium channel 46 is a shell side of the third wound tube heat exchanger 4a, and the third wound tube heat exchanger 4a is a single-flow wound tube heat exchanger having one shell side and one tube side. The fourth heat medium passage 47 is the tube side of the fourth wound tube heat exchanger 4b, the fourth cold medium passage 48 is the shell side of the fourth wound tube heat exchanger 4b, and the fourth wound tube heat exchanger 4b is a single-flow wound tube heat exchanger having one shell side and one tube side.

The connection structure between the first heat exchange device 4 and each pipeline, the second heat exchange device 5 and the hot high-pressure gas distribution output end 81 in the embodiment is as follows: a third cold medium channel inlet connecting pipe 461 in the third winding pipe type heat exchanger 4a is connected with the output end of the first pipeline 1, a third cold medium channel outlet connecting pipe 462 is connected with a first cold medium channel inlet connecting pipe 521 in the second heat exchanging device 5, a hot high-pressure gas output end 81 is connected with the output end of the third pipeline 3 and then connected with a third hot medium channel inlet connecting pipe 451, a third hot medium channel outlet connecting pipe 452 is connected with a fourth hot medium channel inlet connecting pipe 471 in the fourth winding pipe type heat exchanger 4b, the fourth hot medium channel outlet connecting pipe 472 is connected with a second downstream device 9, the fourth cold medium channel inlet connecting pipe 481 is connected with the output end of the second pipeline 2, and the fourth cold medium channel outlet connecting pipe 482 is connected with a second cold medium channel inlet connecting pipe 531 in the second heat exchanging device 5.

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 a shell pass of a third wound tube type heat exchanger 4a and one tube pass of a second heat exchange device 5 and then outputting the mixture from the second heat exchange device 5, 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 heat exchange device 5 is 330-388 ℃; and the low-fraction oil in the second pipeline 2 sequentially passes through the shell pass of the fourth wound-tube heat exchanger 4b and the other tube pass of the second heat exchange device 5 and then is output from the second heat exchange device 5, the temperature of the low-fraction oil in the second pipeline 2 is 55 ℃, the temperature of the low-fraction oil from the second heat exchange device 5 is 185-207 ℃, and the low-fraction oil is sent to the first downstream equipment. The mixture from the second heat exchange device 5 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 taken as a heat medium of the second heat exchange device 5 to pass through the shell pass of the second heat exchange device 5 and exchange heat with the medium in the tube pass of the second heat exchange device 5, the temperature of the reaction product from the second heat exchange device 5 is reduced to 230 ℃, the reaction product enters a thermal high-pressure separation tank 8 to separate thermal high-pressure gas and thermal high-pressure oil, the separated thermal high-pressure gas is mixed with water in a third pipeline 3 and then sequentially passes through the tube passes of a third wound tube type heat exchanger 4a and a fourth wound tube type heat exchanger 4b to exchange heat with the medium in the shell passes of the third wound tube type heat exchanger 4a and the fourth wound tube type heat exchanger 4b, the temperature of the thermal high-pressure gas and the water from the fourth wound tube type heat exchanger 4b is reduced to 105 ℃, and then enters a second downstream device 9.

Example three:

as shown in fig. 3, a third preferred embodiment of a hydrogenation heat exchange system using a multi-stream wound tube heat exchanger according to the present invention is substantially the same as the first embodiment, except that the first heat exchange device 4 in the present embodiment is slightly different from the first heat exchange device in the first embodiment, the first heat exchange device 4 in the present embodiment has one first heat medium channel 41 and three first cold medium channels, and the first heat exchange device 4 is further provided with a first cold medium channel three-inlet connection pipe 441 and a first cold medium channel three-outlet connection pipe 442 which are communicated with the first cold medium channel three 44. Meanwhile, the present embodiment further includes a fourth pipeline 30 for transporting water, the first cooling medium channel three inlet connection pipe 441 is connected to an output end of the fourth pipeline 30, and the first cooling medium channel three outlet connection pipe 442 is connected to the 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 first cold medium channel three outlet connecting pipe 442 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 and the low oil in the second pipeline 2 are sequentially input into corresponding tube passes in the first heat exchange device 4 and the second heat exchange device 5, the water in the fourth pipeline 30 is input into corresponding tube passes in the first heat exchange device 4, the temperature of the mixture in the first pipeline 1 is 130 ℃, the temperature of the low oil in the second pipeline 2 is 55 ℃, the temperatures of the mixture and the low oil from the second heat exchange device 5 are 330-388 ℃, 185-207 ℃, the temperature of the water in the fourth pipeline 30 is 70 ℃, the temperature of the water from the first heat exchange device 4 is 95 ℃, and the water is sent to a third downstream device. The mixture from the second heat exchange device 5 passes through the heating furnace 6 and the 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 taken as a heat medium of the second heat exchange device 5 to pass through the shell pass of the second heat exchange device 5 and exchange heat with the medium in the tube pass of the second heat exchange device 5, the temperature of the reaction product from the second heat exchange device 5 is reduced to 230 ℃, the reaction product enters the thermal high separation tank 8 to separate thermal high-pressure gas and thermal high-pressure oil, the separated thermal high-pressure gas is mixed with water in the third pipeline 3 and then taken as a heat medium of the first heat exchange device 4 to pass through the shell pass of the first heat exchange device 4 and exchange heat with the medium in the tube pass of the first heat exchange device 4, and the temperature of the thermal high-pressure gas and the water from the first heat exchange device 4 is reduced to 95 ℃, and then the mixture enters the second downstream equipment 9.

Example four:

as shown in fig. 4, a fourth preferred embodiment of the hydrogenation heat exchange system using a multi-stream wound tube heat exchanger of the present invention is substantially the same as the second embodiment, except that a fourth pipeline 30 for conveying water and a fifth wound tube heat exchanger 50 are further included in the present embodiment, the fifth wound tube heat exchanger 50 has a fifth heat medium passage 501 and a fifth cooling medium passage 502, and a fifth refrigerant channel inlet connection pipe 503 and a fifth refrigerant channel outlet connection pipe 504 which are communicated with the fifth refrigerant channel 502 are arranged on the fifth wound tube type heat exchanger 50, the fifth refrigerant channel inlet connection pipe 503 is connected with the output end of the fourth pipeline 30, the fifth refrigerant channel outlet connection pipe 504 is connected to the third downstream equipment, and the fourth heat medium channel outlet connection pipe 472 in the fourth wound tube type heat exchanger 4b is connected to the second downstream equipment 9 through the fifth heat medium channel 501.

In this embodiment, the fifth heat medium channel 501 is a tube side of the fifth wound tube heat exchanger 50, the fifth cooling medium channel 502 is a shell side of the fifth wound tube heat exchanger 50, and the fifth wound tube heat exchanger 50 is a single-flow wound tube heat exchanger having one shell side and one tube side.

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 the shell pass of the third wound tubular heat exchanger 4a and one tube pass of the second heat exchange device 5 and then is output from the second heat exchange device 5, the temperature of the mixture in the first pipeline 1 is 130 ℃, and the temperature of the mixture from the second heat exchange device 5 is 330-388 ℃; and the low-fraction oil in the second pipeline 2 sequentially passes through the shell pass of the fourth wound-tube heat exchanger 4b and the other tube pass of the second heat exchange device 5 and then is output from the second heat exchange device 5, the temperature of the low-fraction oil in the second pipeline 2 is 55 ℃, the temperature of the low-fraction oil from the second heat exchange device 5 is 185-207 ℃, and the low-fraction oil is sent to the first downstream equipment. The water in the fourth line 30 (water temperature 55 c) is fed to the shell side of the fifth wound tube heat exchanger 50 and the water exiting the fifth wound tube heat exchanger 50 is at a temperature of 95 c and then sent to the third downstream equipment. The mixture from the second heat exchange device 5 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 taken as a heat medium of the second heat exchange device 5 to go through the shell pass of the second heat exchange device 5 and exchange heat with the medium in the tube pass of the second heat exchange device 5, the temperature of the reaction product from the second heat exchange device 5 is reduced to 230 ℃, the reaction product enters a thermal high separation tank 8 to separate thermal high-pressure gas and thermal high-pressure oil, the separated thermal high-pressure gas is mixed with water in a third pipeline 3 and then is taken as a heat medium to sequentially pass through the tube passes of a third wound tube type heat exchanger 4a, a fourth wound tube type heat exchanger 4b and a fifth wound tube type heat exchanger 50 to exchange heat with the medium in the shell pass of the third wound tube type heat exchanger 4a, the fourth wound tube type heat exchanger 4b and the fifth wound tube type heat exchanger 50, the temperature of the hot high-pressure gas and water from the fifth coiled pipe heat exchanger 50 is reduced to 105 ℃, and then the hot high-pressure gas and water enters the second downstream equipment 9.

Example five:

as shown in fig. 5, a fifth preferred embodiment of the hydrogenation heat exchange system using a multi-stream wound tube heat exchanger according to the present invention is substantially the same as the first embodiment, except that a fourth pipeline 30 for transporting water and a fifth wound tube heat exchanger 50 are further included in the present embodiment, the fifth wound tube heat exchanger 50 has a fifth heat medium passage 501 and a fifth cooling medium passage 502, and a fifth refrigerant channel inlet connection pipe 503 and a fifth refrigerant channel outlet connection pipe 504 which are communicated with the fifth refrigerant channel 502 are arranged on the fifth wound tube heat exchanger 50, the fifth refrigerant channel inlet connection pipe 503 is connected with the output end of the fourth pipeline 30, the fifth refrigerant channel outlet connection pipe 504 is connected to the third downstream equipment, and the first heat medium channel outlet connection pipe 412 in the first heat exchange device 4 is connected to the second downstream equipment 9 through the fifth heat medium channel 501.

In this embodiment, the fifth heat medium channel 501 is a tube side of the fifth wound tube heat exchanger 50, the fifth cooling medium channel 502 is a shell side of the fifth wound tube heat exchanger 50, and the fifth wound tube heat exchanger 50 is a single-flow wound tube heat exchanger having one shell side and one tube side.

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 and the low oil in the second pipeline 2 are sequentially input into the corresponding tube passes of the first heat exchange device 4 and the second heat exchange device 5, the temperature of the mixture in the first pipeline 1 is 130 ℃, the temperature of the low oil in the second pipeline 2 is 55 ℃, and the temperatures of the mixture and the low oil from the second heat exchange device 5 are 330-388 ℃ and 185-207 ℃ respectively. The mixture from the second heat exchange device 5 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 taken as a heat medium of the second heat exchange device 5 to pass through the shell pass of the second heat exchange device 5 and exchange heat with the medium in the tube pass of the second heat exchange device 5, the temperature of the reaction product from the second heat exchange device 5 is reduced to 230 ℃, the reaction product enters a thermal high-temperature separation tank 8 to separate thermal high-temperature component gas and thermal high-temperature component oil, the separated thermal high-temperature component gas is mixed with water in a third pipeline 3 and then sequentially passes through the shell pass of the first heat exchange device 4 and the tube pass of the fifth wound tube heat exchanger 50 to exchange heat with the medium in the tube pass of the first heat exchange device 4 and the medium in the shell pass of the fifth wound tube heat exchanger 50, the temperature of the thermal high-temperature component gas and the water from the fifth wound tube heat exchanger 50 is reduced to 95 ℃, and then enters a second downstream device 9. The water in the fourth line 30 (water temperature 55 c) is fed to the shell side of the fifth wound tube heat exchanger 50 and the water exiting the fifth wound tube heat exchanger 50 is at a temperature of 95 c and then sent to the third downstream equipment.

Example six:

as shown in fig. 6, a sixth preferred embodiment of a hydrogenation heat exchange system using a multi-stream wound tube heat exchanger according to the present invention is basically the same as the first embodiment, except that the first heat exchange device in this embodiment is slightly different from the first heat exchange device in the first embodiment, in this embodiment, the first heat medium channel 41 is a tube side of the first heat exchange device 4, the first cold medium channel is a shell side of the first heat exchange device 4, and the first heat exchange device 4 is a wound tube heat exchanger having two shell sides and one tube side.

The second heat exchange device in this embodiment may refer to the structural design of the first heat exchange device in this embodiment, and may also be set up with the structure of the first heat exchange device in the first embodiment, specifically selected according to actual conditions.

Example seven:

as shown in fig. 7, a seventh preferred embodiment of a hydrogenation heat exchange system using a multi-stream wound tube heat exchanger according to the present invention is basically the same as the third embodiment, except that the first heat exchange device in the third embodiment is slightly different from the first heat exchange device in the third embodiment, the first heat medium channel 41 in the present embodiment is a tube side of the first heat exchange device 4, the first cold medium channel is a shell side of the first heat exchange device 4, and the first heat exchange device 4 is a wound tube heat exchanger having three shell sides and one tube side.

Example eight:

as shown in fig. 8, is an eighth preferred embodiment of the hydrogenation heat exchange system using the multi-stream wound tube heat exchanger of the present invention, the hydrogenation heat exchange system is basically the same as the hydrogenation heat exchange system in the first embodiment, except that the second downstream equipment 9 in this embodiment is a wound tube heat exchanger having a hot medium channel 92 and a cold medium channel 91, and further includes a cold water pipeline 100 for transporting cold water, an output end of the cold water pipeline 100 is connected to an inlet connection pipe of the cold medium channel 91 of the second downstream equipment 9, an inlet connection pipe of the hot medium channel 92 of the second downstream equipment 9 is connected to an output end of the first heat exchange device 4 for outputting heat-exchanged hot high-pressure gas (in this embodiment, an output end of the first heat exchange device 4 for outputting heat-exchanged hot high-pressure gas is a first hot medium channel outlet connection pipe 412), and an outlet connection pipe of the hot 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, an output end of the bypass line 110 is connected between an output end of the heating furnace 6 and an input end of the hydrogenation reactor 7, an input end of the bypass line 110 is connected between an input end of the heating furnace 6 and an outlet connection pipe 522 of a second cold medium channel of the second heat exchange device 5, the first valve 120 is disposed on the bypass line 110, and the second valve 130 is disposed between an input end of the heating furnace 6 and an 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 second outlet connection pipe 532 of the second refrigerant channel of the second heat exchange device 5; a third valve 150 is provided on the fifth line 140 and a fourth valve 160 is provided between the input of the fifth line 140 and the output of the 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 an outlet connection pipe 522 of the second cold medium channel of the second heat exchange device 5; 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 method for exchanging heat by adopting the hydrogenation heat exchange system of the embodiment comprises the following steps:

the mixture composed of raw oil and hydrogen in the first pipeline 1 and the low oil in the second pipeline 2 are sequentially input into the corresponding tube passes of the first heat exchange device 4 and the second heat exchange device 5, the temperatures of the raw oil and the hydrogen in the first pipeline 1 are respectively 70 ℃ and 83.4 ℃, the temperature of the low oil in the second pipeline 2 is 55 ℃, and the temperatures of the mixture and the low oil from the second heat exchange device 5 are respectively 330-388 ℃ and 185-207 ℃. The mixture from the second heat exchange device 5 passes through the 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 taken as a heat medium of the second heat exchange device 5 to go through the shell pass of the second heat exchange device 5 and exchange heat with a medium in the tube pass of the second heat exchange device 5, the temperature of the reaction product from the second heat exchange device 5 is reduced to 230 ℃, the reaction product enters the thermal high-pressure separation tank 8 to separate thermal high-pressure gas and thermal high-pressure oil, the separated thermal high-pressure gas is mixed with water in the third pipeline 3 and then is taken as a heat medium of the first heat exchange device 4 to go through the shell pass of the first heat exchange device 4 and exchange heat with a medium in the tube pass of the first heat exchange device 4, the temperature of the thermal high-pressure gas and the water from the first heat exchange device 4 is reduced to 105 ℃, and then the mixture enters the heat medium channel 92 of the downstream equipment second 9, and cold water (the water temperature is lower than 35 ℃) in the cold water pipeline 100 is input into the cold medium channel 91 of the downstream equipment second 9 The temperature of the water from the cold medium channel 91 of the second downstream device 9 is less than 45 ℃, the temperature of the medium from the hot medium channel 92 of the second downstream device 9 is 50 ℃, and the water is sent to a cold high separation tank for separation. The hydrogenation heat exchange system of the embodiment has high heat exchange efficiency, so that the mixture coming out of the second heat exchange device 5 can directly enter the hydrogenation reactor 7 for reaction without being heated by the heating furnace, the heating furnace is only used at the initial stage of operation, and the bypass pipeline 110 can be used at other operation stages.

Example nine:

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 and the low-fraction oil in the second pipeline 2 are sequentially input into the corresponding tube passes of the first heat exchange device 4 and the second heat exchange device 5, the temperature of the mixture in the first pipeline 1 is 70 ℃, the pressure is 4.5MPa, the temperature of the low-fraction oil in the second pipeline 2 is 45 ℃, the pressure is 2.0MPa, and the temperature of the mixture and the low-fraction oil discharged from the second heat exchange device 5 are 320 ℃ and 170 ℃ respectively. The mixture from the second heat exchanger 5 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 is taken as a heat medium of the second heat exchanger 5 to go through the shell pass of the second heat exchanger 5 and exchange heat with a medium in the tube pass of the second heat exchanger 5, the temperature of the reaction product from the second heat exchanger 5 is reduced to 220 ℃, the reaction product enters a thermal high-pressure separation tank 8 to separate thermal high-pressure gas and thermal high-pressure oil, the separated thermal high-pressure gas is mixed with water in a third pipeline 3 and then goes through the shell pass of the first heat exchanger 4 as a heat medium of the first heat exchanger 4 and exchanges heat with the medium in the tube pass of the first heat exchanger 4, and the temperature of the thermal high-pressure gas and the water from the first heat exchanger 4 is reduced to 105 ℃, and then the mixture enters a second downstream device 9.

Example ten:

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 and the low-fraction oil in the second pipeline 2 are sequentially input into the corresponding tube passes of the first heat exchange device 4 and the second heat exchange device 5, the temperature of the mixture in the first pipeline 1 is 165 ℃, the pressure is 19MPa, the temperature of the low-fraction oil in the second pipeline 2 is 65 ℃, the pressure is 1.0MPa, and the temperature of the mixture and the low-fraction oil discharged from the second heat exchange device 5 are 395 ℃ and 215 ℃ respectively. The mixture from the second heat exchanger 5 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 of the second heat exchanger 5 to go through the shell pass of the second heat exchanger 5 and exchange heat with a medium in the tube pass of the second heat exchanger 5, the temperature of the reaction product from the second heat exchanger 5 is reduced to 260 ℃, the reaction product enters a thermal high-pressure separation tank 8 to separate thermal high-pressure gas and thermal high-pressure oil, the separated thermal high-pressure gas is mixed with water in a third pipeline 3 and then goes through the shell pass of the first heat exchanger 4 as a heat medium of the first heat exchanger 4 and exchanges heat with the medium in the tube pass of the first heat exchanger 4, and the temperature of the thermal high-pressure gas and the water from the first heat exchanger 4 is reduced to 105 ℃, and then the mixture enters a second downstream device 9.

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 (13)

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, and is characterized in that:

the heat exchange device comprises a first heat exchange device (4) and a second heat exchange device (5), wherein the first heat exchange device (4) is connected with a first pipeline (1), a second pipeline (2) and a hot high-pressure gas output end (81) of the hot high-pressure gas separation tank (8) for outputting hot high-pressure gas, and is used for carrying out primary heat exchange on the hot high-pressure gas, a mixture in the first pipeline (1) and low-pressure oil in the second pipeline (2); the second heat exchange device (5) is connected with the mixture output end and the low oil separation output end of the first heat exchange device (4) and is used for carrying out secondary heat exchange on the mixture and the low oil separation after primary heat exchange;

the second heat exchange device (5) is a second wound tube type heat exchanger with a second heat medium channel (51) and at least two second cold medium channels, and the second wound tube type heat exchanger is provided with a second heat medium channel inlet connecting pipe (511) and a second heat medium channel outlet connecting pipe (512) which are communicated with the second heat medium channel (51), a second cold medium channel first inlet connecting pipe (521) and a second cold medium channel first outlet connecting pipe (522) which are communicated with a second cold medium channel first (52), a second cold medium channel second inlet connecting pipe (531) and a second cold medium channel second outlet connecting pipe (532) which are communicated with a second cold medium channel second (53); the second heat medium channel inlet connecting pipe (511) is connected with the output end of the hydrogenation reactor (7), the second heat medium channel outlet connecting pipe (512) is connected with the input end of the high heat separation tank (8), the second cold medium channel first inlet connecting pipe (521) is connected with the mixture output end at the tail end of the first heat exchange device (4), the second cold medium channel first outlet connecting pipe (522) is connected with the input end of the heating furnace (6), the second cold medium channel second inlet connecting pipe (531) is connected with the low oil distribution output end at the tail end of the first heat exchange device (4), and the second cold medium channel second outlet connecting pipe (532) is connected to a first downstream device.

2. The hydrogenation heat exchange system of claim 1, wherein: the first heat exchange device (4) is a first wound tube type heat exchanger with a first heat medium channel (41) and at least two first cold medium channels, and the first wound tube type heat exchanger is provided with a first heat medium channel inlet connecting pipe (411) and a first heat medium channel outlet connecting pipe (412) which are communicated with the first heat medium channel (41), a first cold medium channel first inlet connecting pipe (421) and a first cold medium channel first outlet connecting pipe (422) which are communicated with the first cold medium channel I (42), a first cold medium channel second inlet connecting pipe (431) and a first cold medium channel second outlet connecting pipe (432) which are communicated with the first cold medium channel II (43);

the first heat medium channel inlet connecting pipe (411) is connected with a heat high-pressure gas output end (81) of the heat high-pressure separation tank (8) for outputting heat high-pressure gas, the first heat medium channel outlet connecting pipe (412) is connected to a second downstream device (9), the first cold medium channel inlet connecting pipe (421) is connected with the output end of the first pipeline (1), and the second cold medium channel inlet connecting pipe (431) is connected with the output end of the second pipeline (2);

and the first outlet connecting pipe (422) of the first cold medium channel and the second outlet connecting pipe (432) of the first cold medium channel are respectively a mixture output end and a low oil-separating output end at the tail end of the first heat exchange device (4).

3. The hydrogenation heat exchange system of claim 2, wherein: the heat exchanger also comprises a fourth pipeline (30) for conveying water, at least three first cold medium channels in the first heat exchange device (4) are provided, and a first cold medium channel three-inlet connecting pipe (441) and a first cold medium channel three-outlet connecting pipe (442) which are communicated with the first cold medium channel three (44) are further arranged on the first heat exchange device (4); the first cold medium channel three-inlet connecting pipe (441) is connected with the output end of the fourth pipeline (30), and the first cold medium channel three-outlet connecting pipe (442) is connected to a downstream device three;

or, the heat exchanger further comprises a fourth pipeline (30) for conveying water and a fifth wound tube heat exchanger (50), the fifth wound tube heat exchanger (50) is provided with a fifth heat medium channel (501) and at least one fifth cold medium channel (502), the fifth wound tube heat exchanger (50) is provided with a fifth cold medium channel inlet connecting pipe (503) and a fifth cold medium channel outlet connecting pipe (504) which are communicated with the fifth cold medium channel (502), the fifth cold medium channel inlet connecting pipe (503) is connected with the output end of the fourth pipeline (30), the fifth cold medium channel outlet connecting pipe (504) is connected to a third downstream device, and the first heat medium channel outlet connecting pipe (412) in the first heat exchange device (4) is connected to a second downstream device (9) through the fifth heat medium channel (501).

4. The hydrogenation heat exchange system of claim 1, wherein: the first heat exchange device (4) comprises a third wound tube type heat exchanger (4a) with a third heat medium channel (45) and at least one third cold medium channel (46), and a fourth wound tube type heat exchanger (4b) with a fourth heat medium channel (47) and at least one fourth cold medium channel (48), wherein a third heat medium channel inlet connecting pipe (451) and a third heat medium channel outlet connecting pipe (452) which are communicated with the third heat medium channel (45) are arranged on the third wound tube type heat exchanger (4a), a third cold medium channel inlet connecting pipe (461) and a third cold medium channel outlet connecting pipe (462) which are communicated with the third cold medium channel (46) are arranged on the fourth wound tube type heat exchanger (4b), and a fourth heat medium channel inlet connecting pipe (471) and a fourth heat medium channel outlet connecting pipe (472) which are communicated with the fourth heat medium channel (47) are arranged on the fourth wound tube type heat exchanger (4b), A fourth cold medium channel inlet connection pipe (481) and a fourth cold medium channel outlet connection pipe (482) which are communicated with the fourth cold medium channel (48);

the third cold medium channel inlet connecting pipe (461) is connected with the output end of the first pipeline (1), the third hot medium channel inlet connecting pipe (451) is connected with a hot high-split gas output end (81) of the hot high-split gas separating tank (8) for outputting hot high-split gas, the third hot medium channel outlet connecting pipe (452) is connected with the fourth hot medium channel inlet connecting pipe (471), the fourth hot medium channel outlet connecting pipe (472) is connected to a second downstream device (9), and the fourth cold medium channel inlet connecting pipe (481) is connected with the output end of the second pipeline (2);

and the third cold medium channel outlet connecting pipe (462) and the fourth cold medium channel outlet connecting pipe (482) are a mixture output end and a low oil separation output end at the tail end of the first heat exchange device (4) respectively.

5. The hydrogenation heat exchange system of claim 4, wherein: the water heater further comprises a fourth pipeline (30) used for conveying water and a fifth wound tube type heat exchanger (50), the fifth wound tube type heat exchanger (50) is provided with a fifth heat medium channel (501) and at least one fifth cold medium channel (502), a fifth cold medium channel inlet connecting pipe (503) and a fifth cold medium channel outlet connecting pipe (504) which are communicated with the fifth cold medium channel (502) are arranged on the fifth wound tube type heat exchanger (50), the fifth cold medium channel inlet connecting pipe (503) is connected with the output end of the fourth pipeline (30), the fifth cold medium channel outlet connecting pipe (504) is connected to a third downstream device, and a fourth heat medium channel outlet connecting pipe (472) in the fourth wound tube type heat exchanger (4b) is connected to a second downstream device (9) through the fifth heat medium channel (501).

6. A hydrogenation heat exchange system according to any one of claims 1 to 5, characterized in that: the second heat medium channel (51) is a shell pass of the second wound tube heat exchanger, the second cold medium channel is a tube pass of the second wound tube heat exchanger, and the second heat exchange device (5) is a double-flow wound tube heat exchanger with one shell pass and two tube passes.

7. The hydrogenation heat exchange system of claim 2, wherein: the first heat medium channel (41) is a shell pass of the first wound tube heat exchanger, the first cold medium channel is a tube pass of the first wound tube heat exchanger, and the first heat exchange device (4) is a double-flow wound tube heat exchanger with one shell pass and two tube passes.

8. The hydrogenation heat exchange system of claim 5, wherein: the third heat medium channel (45) is the tube side of the third wound tube heat exchanger (4a), the third cold medium channel (46) is the shell side of the third wound tube heat exchanger (4a), and the third wound tube heat exchanger (4a) is a single-flow wound tube heat exchanger having one shell side and one tube side;

the fourth heat medium channel (47) is a tube side of the fourth wound tube heat exchanger (4b), the fourth cold medium channel (48) is a shell side of the fourth wound tube heat exchanger (4b), and the fourth wound tube heat exchanger (4b) is a single-flow wound tube heat exchanger having one shell side and one tube side;

the fifth heat medium channel (501) is a tube side of the fifth wound tube heat exchanger (50), the fifth cooling medium channel (502) is a shell side of the fifth wound tube heat exchanger (50), and the fifth wound tube heat exchanger (50) is a single-flow wound tube heat exchanger having one shell side and one tube side.

9. The hydrogenation heat exchange system according to any one of claims 1 to 3, wherein: the heat exchange system is characterized by further comprising a third pipeline (3) used for conveying water, wherein a heat high-pressure gas output end (81) of the heat high-pressure separation tank (8) used for outputting heat high-pressure gas is connected with the output end of the third pipeline (3) and then connected with the first heat exchange device (4).

10. A hydrogenation heat exchange system according to any one of claims 2 to 5, wherein: the second downstream equipment (9) is a high-pressure air cooler;

or the downstream equipment II (9) is a wound tube type heat exchanger with a heat medium channel (92) and at least one cold medium channel (91), and further comprises a cold water pipeline (100) for conveying cold water, the output end of the cold water pipeline (100) is connected with the inlet connecting pipe of the cold medium channel (91) of the downstream equipment II (9), the inlet connecting pipe of the heat medium channel (92) of the downstream equipment II (9) is connected with the output end of the first heat exchange device (4) for outputting heat-exchanged high-pressure gas, and the outlet connecting pipe of the heat medium channel (92) is connected to the cold high separation tank (93).

11. A hydrogenation heat exchange system according to any one of claims 1 to 5, characterized in that: the heat exchanger is characterized by further comprising a bypass pipeline (110), a first valve (120) and a second valve (130), wherein the output end of the bypass pipeline (110) is connected between the output end of the heating furnace (6) and the input end of the hydrogenation reactor (7), the input end of the bypass pipeline (110) is connected between the input end of the heating furnace (6) and an outlet connecting pipe (522) of a second cold medium channel of the second heat exchange device (5), the first valve (120) is arranged on the bypass pipeline (110), and the second valve (130) is arranged between the input end of the heating furnace (6) and the input end of the bypass pipeline (110).

12. A hydrogenation heat exchange system according to any one of claims 1 to 5, characterized in that: the heat exchanger also comprises a fifth pipeline (140), a third valve (150) and a fourth valve (160), wherein the input end of the fifth pipeline (140) is connected with the second pipeline (2), and the output end of the fifth pipeline is connected with a second outlet connecting pipe (532) of a second cold medium channel of the second heat exchange device (5); the third valve (150) is 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).

13. A hydrogenation heat exchange system according to any one of claims 1 to 5, characterized in that: 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 an outlet connecting pipe (522) of a second cold medium channel of the second heat exchange device (5); 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).

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