CN113532156B

CN113532156B - Atmospheric and vacuum heat exchange system with winding tube type heat exchanger

Info

Publication number: CN113532156B
Application number: CN202110927921.2A
Authority: CN
Inventors: 马慧丽; 胡兴苗; 任红亮; 王健良; 陈福潭; 王宇; 陶江; 徐伟栋
Original assignee: Zhenhai Petrochemical Construction And Installation Engineering Co ltd
Current assignee: Zhenhai Petrochemical Construction And Installation Engineering Co ltd
Priority date: 2021-08-11
Filing date: 2021-08-11
Publication date: 2024-06-04
Anticipated expiration: 2041-08-11
Also published as: CN113532156A

Abstract

An atmospheric and vacuum heat exchange system with a winding pipe type heat exchanger comprises a first heat exchanger group (E1), a first electric desalting device (1), a second heat exchanger group (E2), a first primary distillation tower (2), a third heat exchanger group (E3), a stripping tower (9), an atmospheric tower (3) and a vacuum tower (4), and also comprises a fourth heat exchanger group (E4), a second electric desalting device (5), a fifth heat exchanger group (E5), a second primary distillation tower (6) and a sixth heat exchanger group (E6); the second primary bottom oil output end at the tail end of the sixth heat exchanger group is sequentially connected with the atmospheric tower (3) and the vacuum tower (4), and oil discharged from the first primary tower (2) or/and the second primary tower (6) or/and the atmospheric tower (3) or/and the vacuum tower (4) is connected with the fourth, fifth and sixth heat exchanger groups according to the required working condition. Compared with the prior art, the application can process two different crude oils simultaneously and simplify the heat exchange network.

Description

Atmospheric and vacuum heat exchange system with winding tube type heat exchanger

Technical Field

The invention belongs to the technical field of oil refining devices and processes, and particularly relates to an atmospheric and vacuum heat exchange system with a winding tube type heat exchanger.

Background

The atmospheric and vacuum heat exchange system is generally provided with an atmospheric distillation device, a vacuum distillation device and a heat exchange device and mainly comprises the desalination and dehydration of crude oil; atmospheric distillation; and vacuum distillation. At present, the heat exchange devices in the atmospheric and vacuum heat exchange system are mainly plate heat exchangers, shell-and-tube heat exchangers and other common heat exchangers, such as a scheme disclosed in patent application No. CN201610978721.9, a normal-pressure high-efficiency energy-saving deep drawing process based on clear cutting (application publication No. CN 107057747A), and the common heat exchangers are large in required quantity, complex in piping and large in occupied area.

In order to simplify the heat exchange system, the inventor adopts a multi-stream winding tube type heat exchanger to replace a common heat exchanger, and simplifies and optimizes the heat exchange system and the heat exchange process, such as the scheme disclosed in patent number ZL201410802568.5, namely an atmospheric and vacuum device heat exchange system and process (issued publication number CN 104479735B) and patent application number CN201910687963.6, namely an atmospheric and vacuum heat exchange system with winding tube type heat exchanger and heat exchange process (applied publication number CN 110373222A), and the number of heat exchange devices in the heat exchange systems is greatly reduced.

However, in the existing atmospheric and vacuum heat exchange system, only one crude oil can be processed, and if two different crude oils are to be processed at the same time, the number of heat exchange devices needs to be greatly increased, so that a heat exchange network is complex.

Disclosure of Invention

The invention aims to solve the first technical problem of providing an atmospheric and vacuum heat exchange system with a winding pipe type heat exchanger, which can process two different crude oils simultaneously and can simplify a heat exchange network.

The second technical problem to be solved by the invention is to provide a heat exchange process for exchanging heat by adopting the atmospheric and vacuum heat exchange system, so that the heat exchange process is simplified, and the heat loss is reduced.

The technical scheme adopted by the invention for solving the first technical problem is as follows: an atmospheric and vacuum heat exchange system with a wound tube heat exchanger comprises a first heat exchanger group for carrying out primary heat exchange on first crude oil; a first electrical desalting device connected with a first crude oil output end at the tail end of the first heat exchanger group; the second heat exchanger group is connected with the output end of the first electric desalting device and is used for carrying out secondary heat exchange on the first desalted crude oil obtained after desalting; the first primary distillation tower is connected with the first crude oil output end after the first stripping at the tail end of the second heat exchanger group; the third heat exchanger group is connected with the bottom of the first primary distillation tower and is used for carrying out tertiary heat exchange on the first primary bottom oil obtained after the primary distillation of the crude oil after the first removal; the stripping tower, the atmospheric tower and the vacuum tower are sequentially connected with the first primary bottom oil output end at the tail end of the third heat exchanger group, and oil from the first primary distillation tower or/and the atmospheric tower or/and the vacuum tower or/and the stripping tower is connected with the first heat exchanger group, the second heat exchanger group and the third heat exchanger group according to the required working conditions so as to heat the first crude oil, the first separated crude oil and the first primary bottom oil; at least part of heat exchangers in the first heat exchanger group or/and the second heat exchanger group or/and the third heat exchanger group are wound tube heat exchangers;

The method is characterized in that: the system also comprises a fourth heat exchanger group for carrying out primary heat exchange on the second crude oil; a second electrical desalting device connected with the second crude oil output end at the tail end of the fourth heat exchanger group; the fifth heat exchanger group is connected with the output end of the second electric desalting device and is used for carrying out secondary heat exchange on the second desalted crude oil obtained after desalting; the second primary distillation tower is connected with the second crude oil output end after the removal at the tail end of the fifth heat exchanger group; the sixth heat exchanger group is connected with the bottom of the second primary distillation tower and is used for carrying out tertiary heat exchange on second primary bottom oil obtained after the primary distillation of the second crude oil after the removal; the second primary bottom oil output end at the tail end of the sixth heat exchanger set is sequentially connected with the atmospheric tower and the vacuum tower, and the oil content from the first primary distillation tower or/and the second primary distillation tower or/and the atmospheric tower or/and the vacuum tower is connected with the fourth heat exchanger set, the fifth heat exchanger set and the sixth heat exchanger set according to the required working conditions so as to heat the second crude oil, the second crude oil after the second separation and the second primary bottom oil; at least part of heat exchangers in the fourth heat exchanger group or/and the fifth heat exchanger group or/and the sixth heat exchanger group are wound tube heat exchangers.

Preferably, the winding tube heat exchanger is at least one of a single-flow winding tube heat exchanger, a double-flow winding tube heat exchanger, a three-flow winding tube heat exchanger and a four-flow winding tube heat exchanger, the single-flow winding tube heat exchanger is a heat exchanger with one shell side and one tube side, the double-flow winding tube heat exchanger is a heat exchanger with one shell side and two tube sides, the three-flow winding tube heat exchanger is a heat exchanger with one shell side and three tube sides, and the four-flow winding tube heat exchanger is a heat exchanger with one shell side and four tube sides.

Preferably, the first heat exchanger group comprises a double-flow winding tube type heat exchanger I, a four-flow winding tube type heat exchanger II and a single-flow heat exchanger III, wherein the single-flow heat exchanger III is a heat exchanger with one heat medium channel and one cold medium channel;

The second heat exchanger group comprises a three-flow winding tubular heat exchanger IV and a four-flow winding tubular heat exchanger V;

The third heat exchanger group comprises a single-flow heat exchanger six and a double-flow winding tube heat exchanger seven, wherein the single-flow heat exchanger six is a heat exchanger with one heat medium channel and one cold medium channel;

the fourth heat exchanger group comprises a first single-flow winding tube type heat exchanger, a second double-flow winding tube type heat exchanger and a third three-flow winding tube type heat exchanger;

The fifth heat exchanger group comprises a fourth single-flow heat exchanger, a fifth three-flow winding tube heat exchanger and a sixth single-flow heat exchanger, wherein the fourth single-flow heat exchanger is a heat exchanger with one heat medium channel and one cold medium channel, and the sixth single-flow heat exchanger is a heat exchanger with one heat medium channel and one cold medium channel;

The sixth heat exchanger group comprises a seventh double-flow winding tube type heat exchanger;

The first pipeline for accessing the first crude oil is sequentially connected with a shell side of the double-flow winding tubular heat exchanger I, a shell side of the four-flow winding tubular heat exchanger II and a cold medium channel of the single-flow heat exchanger III, and then is connected with the first electric desalting device; the pipeline of the first electric desalting device is sequentially connected with the shell pass of the three-stream winding tube type heat exchanger IV and the shell pass of the four-stream winding tube type heat exchanger V, then is connected with the first primary distillation tower, the first pipeline which is used for conveying first primary bottom oil and comes out of the bottom of the first primary distillation tower is sequentially connected with the cold medium channel of the single-stream heat exchanger V and the shell pass of the double-stream winding tube type heat exchanger V, then is connected with the stripping tower, and the top output end of the stripping tower is sequentially connected with the atmospheric tower and the vacuum tower;

The second pipeline for accessing the second crude oil is sequentially connected with the shell side of the first single-flow winding tubular heat exchanger, the shell side of the second double-flow winding tubular heat exchanger and the shell side of the third double-flow winding tubular heat exchanger, and then is connected with a second electric desalting device; the pipeline of the second electric desalting device is sequentially connected with a cold medium channel of a fourth single-flow heat exchanger, a shell side of a fifth three-flow winding tube type heat exchanger and a cold medium channel of a sixth single-flow heat exchanger, then is connected with a second primary distillation tower, and a second pipeline which is used for conveying second primary bottom oil and comes out of the bottom of the second primary distillation tower is connected with the shell side of a seventh double-flow winding tube type heat exchanger, and then is sequentially connected with the atmospheric tower and the vacuum tower;

A first top pipeline at the top of the first primary distillation tower is connected with a first tube pass of the double-flow winding tube type heat exchanger I and then connected with the downstream; the circulating pipeline I at the top of the first preliminary distillation tower is connected with the second tube pass of the four-stream winding tube type heat exchanger II and returns to the first preliminary distillation tower;

A second top pipeline at the top of the second primary distillation tower is connected with the tube pass of the first single-flow winding tube type heat exchanger and then connected with the downstream; a second circulating pipeline at the top of the second primary distillation tower is connected with a second tube pass of the second double-stream winding tube type heat exchanger and returns to the second primary distillation tower;

the top circulation pipeline at the top of the atmospheric tower is sequentially connected with the first tube pass of the four-flow winding tube heat exchanger II and the first tube pass of the second double-flow winding tube heat exchanger and returns to the atmospheric tower;

the normal top oil gas pipeline at the top of the atmospheric tower is connected with the second tube pass of the double-flow winding tube type heat exchanger I and then connected with the downstream;

the first pipeline at the top of the atmospheric tower is sequentially connected with the aviation kerosene hydrogenation device, the third tube side of the fifth three-flow winding tube type heat exchanger, the second tube side of the third three-flow winding tube type heat exchanger and the fourth tube side of the four-flow winding tube type heat exchanger, and then returns to the aviation kerosene hydrogenation device;

the second side line at the upper part of the atmospheric tower is sequentially connected with the first tube pass of the fifth three-stream winding tube heat exchanger and is connected with the downstream after the third tube pass of the fourth-stream winding tube heat exchanger;

the third side line in the middle of the atmospheric tower is sequentially connected with the fourth tube pass of the four-stream winding tube heat exchanger five, the heat medium channel of the fourth single-stream heat exchanger and the third tube pass of the third three-stream winding tube heat exchanger and then connected with the downstream;

The first circulating pipeline of the atmospheric tower is sequentially connected with the first tube pass of the three-flow winding tube type heat exchanger IV and returns to the atmospheric tower;

the second circulating pipeline of the atmospheric tower is sequentially connected with the heat medium channel of the single-flow heat exchanger six and the first tube pass of the four-flow winding tube type heat exchanger five and returns to the atmospheric tower;

A first heavy oil pipeline at the bottom of the stripping tower, which is used for outputting first heavy oil obtained after the first crude oil is stripped, is sequentially connected with a first tube pass of a double-flow winding tube heat exchanger seven, a first tube pass of a seventh double-flow winding tube heat exchanger, a second tube pass of a fifth three-flow winding tube heat exchanger and a first tube pass of a third three-flow winding tube heat exchanger and then is connected to the downstream;

The slag reducing pipeline at the bottom of the vacuum tower is sequentially connected with the second tube pass of the double-flow winding tube type heat exchanger seven and the heat medium channel of the sixth single-flow heat exchanger and then divided into two strands, namely a first slag reducing pipeline for conveying vacuum residue and a second slag reducing pipeline for conveying quenching oil, wherein the first slag reducing pipeline is sequentially connected with the third tube pass of the four-flow winding tube type heat exchanger five and the heat medium channel of the third single-flow heat exchanger three and then connected with the downstream; the second strand slag reducing pipeline returns to the vacuum tower;

A third pipeline in the middle of the vacuum tower is sequentially connected with a second tube pass of a seventh double-flow winding tube heat exchanger and a second tube pass of a fourth-flow winding tube heat exchanger and then divided into two strands, wherein the first strand of third pipeline is connected with the third tube pass of the fourth-flow winding tube heat exchanger and then connected with the downstream, and the second strand of third pipeline returns to the vacuum tower;

The second pipeline at the upper part of the vacuum tower is connected with the second tube pass of the three-flow winding tube type heat exchanger four and then is divided into two strands, wherein the first strand of second pipeline is connected with the downstream, and the second strand of second pipeline returns to the vacuum tower.

Also preferably, the first heat exchanger group includes a single-flow wound tube heat exchanger one, a single-flow wound tube heat exchanger two, a four-flow wound tube heat exchanger two and a single-flow heat exchanger three, wherein the single-flow heat exchanger three is a heat exchanger with one heat medium channel and one cold medium channel;

The first pipeline for accessing the first crude oil is divided into two branches, and is respectively connected with the shell side of the single-flow winding tubular heat exchanger I and the shell side of the single-flow winding tubular heat exchanger II, then sequentially connected to the shell side of the four-flow winding tubular heat exchanger II and the cold medium channel of the single-flow heat exchanger III, and then connected with the first electric desalting device; the pipeline of the first electric desalting device is sequentially connected with the shell pass of the three-stream winding tube type heat exchanger IV and the shell pass of the four-stream winding tube type heat exchanger V, then is connected with the first primary distillation tower, the first pipeline which is used for conveying first primary bottom oil and comes out of the bottom of the first primary distillation tower is sequentially connected with the cold medium channel of the single-stream heat exchanger V and the shell pass of the double-stream winding tube type heat exchanger V, then is connected with the stripping tower, and the top output end of the stripping tower is sequentially connected with the atmospheric tower and the vacuum tower;

The second pipeline for accessing the second crude oil is sequentially connected with the shell side of the first single-flow winding tubular heat exchanger, the shell side of the second double-flow winding tubular heat exchanger and the shell side of the third double-flow winding tubular heat exchanger, and then is connected with a second electric desalting device; the pipeline from the second electric desalting device is sequentially connected with a cold medium channel of a fourth single-flow heat exchanger, a shell side of a fifth three-flow winding pipe type heat exchanger and a cold medium channel of a sixth single-flow heat exchanger, then is connected with a second primary distillation tower, and a pipeline from the bottom of the second primary distillation tower for conveying second primary bottom oil is connected with the shell side of a seventh double-flow winding pipe type heat exchanger, and then is sequentially connected with the atmospheric tower and the vacuum tower;

a first top pipeline at the top of the first primary distillation tower is connected with the tube pass of the single-flow winding tube type heat exchanger II and then connected with the downstream; the circulating pipeline I at the top of the first preliminary distillation tower is connected with the second tube pass of the four-stream winding tube type heat exchanger II and returns to the first preliminary distillation tower;

The normal top oil gas pipeline at the top of the atmospheric tower is connected with the tube pass of the single-flow winding tube type heat exchanger I and then connected with the downstream;

In the scheme, the third single-flow heat exchanger is a single-flow winding tube type heat exchanger or a plate type heat exchanger or a common tube type heat exchanger; the single-flow heat exchanger is a single-flow winding tube heat exchanger or a plate heat exchanger or a common tube type heat exchanger; the fourth single-flow heat exchanger is a single-flow winding tube heat exchanger or a plate heat exchanger or a common tube type heat exchanger; the sixth single-flow heat exchanger is a single-flow winding tube type heat exchanger or a plate type heat exchanger or a common tube type heat exchanger;

The technical scheme adopted by the invention for solving the first technical problem can be as follows: an atmospheric and vacuum heat exchange system with a wound tube heat exchanger comprises a first heat exchanger group for carrying out primary heat exchange on first crude oil; a first electrical desalting device connected with a first crude oil output end at the tail end of the first heat exchanger group; the second heat exchanger group is connected with the output end of the first electric desalting device and is used for carrying out secondary heat exchange on the first desalted crude oil obtained after desalting; a primary distillation tower connected with the first crude oil output end of the second heat exchanger group; the third heat exchanger group is connected with the bottom of the primary distillation tower and is used for carrying out tertiary heat exchange on the first primary bottom oil obtained after the primary distillation of the first crude oil after the first removal; the stripping tower, the atmospheric tower and the vacuum tower are sequentially connected with the first primary bottom oil output end at the tail end of the third heat exchanger group, and oil from the first primary distillation tower or/and the atmospheric tower or/and the vacuum tower or/and the stripping tower is connected with the first heat exchanger group, the second heat exchanger group and the third heat exchanger group according to the required working conditions so as to heat the first crude oil, the first separated crude oil and the first primary bottom oil; at least part of heat exchangers in the first heat exchanger group or/and the second heat exchanger group or/and the third heat exchanger group are wound tube heat exchangers;

The method is characterized in that: a partition board is vertically arranged in the primary distillation tower, the partition board is arranged at the lower part of the primary distillation tower, the space at the lower part of the primary distillation tower is divided into two parts, namely a first space and a second space, the first space and the second space are communicated with the space at the upper part of the primary distillation tower, and a first crude oil output end at the tail end of the second heat exchanger group after the first separation is connected to the first space at the lower part of the primary distillation tower; the bottom of the first space is connected with the input end of the third heat exchanger group;

The system also comprises a fourth heat exchanger group for carrying out primary heat exchange on the second crude oil; a second electrical desalting device connected with the second crude oil output end at the tail end of the fourth heat exchanger group; the fifth heat exchanger group is connected with the output end of the second electric desalting device and is used for carrying out secondary heat exchange on the second desalted crude oil obtained after desalting; the second crude oil output end after the removal at the tail end of the fifth heat exchanger group is connected to the second space at the lower part of the primary distillation tower;

The second heat exchanger group is connected with the bottom of the second space of the primary distillation tower and is used for carrying out tertiary heat exchange on the second primary bottom oil obtained after the primary distillation of the second crude oil after the removal; the second primary bottom oil output end at the tail end of the sixth heat exchanger group is sequentially connected with the atmospheric tower and the vacuum tower, and the oil content from the primary distillation tower or/and the atmospheric tower or/and the vacuum tower or/and the stripping tower is connected with the fourth heat exchanger group, the fifth heat exchanger group and the sixth heat exchanger group according to the required working conditions so as to heat the second crude oil, the second separated crude oil and the second primary bottom oil; at least part of heat exchangers in the fourth heat exchanger group or/and the fifth heat exchanger group or/and the sixth heat exchanger group are wound tube heat exchangers.

Preferably, the first heat exchanger group comprises a four-flow winding tube type heat exchanger I and a double-flow winding tube type heat exchanger II;

the second heat exchanger group comprises four-flow winding tube type heat exchangers III;

The third heat exchanger group comprises a three-flow winding tube heat exchanger IV and a double-flow winding tube heat exchanger V;

The fourth heat exchanger group comprises a I single-flow winding tubular heat exchanger, a II single-flow winding tubular heat exchanger and a III double-flow winding tubular heat exchanger;

The fifth heat exchanger group comprises an IV third-stream winding tube type heat exchanger and a V single-stream heat exchanger, and the V single-stream heat exchanger is a heat exchanger with a heat medium channel and a cold medium channel;

The sixth heat exchanger group comprises a VI third-strand flow winding tubular heat exchanger and a VII double-strand flow winding tubular heat exchanger;

The first pipeline for accessing the first crude oil is sequentially connected with the shell pass of the four-stream winding tubular heat exchanger I and the shell pass of the double-stream winding tubular heat exchanger II, and then is connected with the first electric desalting device; the pipeline of the first electric desalting device is connected with the shell side of the four-flow winding tubular heat exchanger III, then is connected with the first space of the primary distillation tower, the first pipeline which is used for conveying first primary bottom oil and comes out of the bottom of the first space is sequentially connected with the shell side of the three-flow winding tubular heat exchanger IV and the shell side of the double-flow winding tubular heat exchanger V, then is connected with the stripping tower, and the top output end of the stripping tower is sequentially connected with the atmospheric tower and the vacuum tower;

The second pipeline for accessing the second crude oil is sequentially connected with the shell side of the I single-flow winding tubular heat exchanger, the shell side of the II single-flow winding tubular heat exchanger and the shell side of the III double-flow winding tubular heat exchanger, and then is connected with a second electric desalting device; the pipeline from the second electric desalting device is divided into two paths, and is respectively connected with the shell side of the IV third-stream winding tubular heat exchanger and the cold medium channel of the V single-stream heat exchanger, then is connected with the second space of the primary distillation tower, and the pipeline from the bottom of the second space for conveying second primary bottom oil is sequentially connected with the shell side of the VI third-stream winding tubular heat exchanger and the shell side of the VII double-stream winding tubular heat exchanger, and then is sequentially connected with the atmospheric tower and the vacuum tower;

The top pipeline at the top of the primary distillation tower is connected with the tube pass of the II single-flow winding tube type heat exchanger and then connected with the downstream; a circulating pipeline at the top of the primary distillation tower is connected with the first tube pass of the III double-flow winding tube type heat exchanger and returns to the primary distillation tower;

the top circulating pipeline at the top of the atmospheric tower is connected with the fourth tube pass of the four-flow winding tube type heat exchanger I and returns to the atmospheric tower;

the top circulation pipeline at the top of the atmospheric tower is connected with the second tube pass of the III double-flow winding tube type heat exchanger and returns to the atmospheric tower;

the normal top oil gas pipeline at the top of the atmospheric tower is connected with the tube pass of the I single-flow winding tube type heat exchanger and then connected with the downstream;

the third side line of the atmospheric tower is sequentially connected with the first tube pass of the VII double-flow winding tube heat exchanger and the second tube pass of the VI third-flow winding tube heat exchanger and then connected with the downstream;

The first circulating pipeline of the atmospheric tower is connected with the heat medium channel of the V single-stream heat exchanger and returns to the atmospheric tower;

The second circulating pipeline of the atmospheric tower is connected with a third tube pass of the VI third stream winding tube type heat exchanger and returns to the atmospheric tower;

The first pipeline at the top of the atmospheric tower is sequentially connected with the aviation kerosene hydrogenation device, the first tube pass of the IV third-stream winding tube type heat exchanger and the second tube pass of the four-stream winding tube type heat exchanger I, and then returns to the aviation kerosene hydrogenation device;

a heavy oil pipeline I at the bottom of the stripping tower, which is used for outputting heavy oil I obtained after the first crude oil is stripped, is connected with a first tube pass of a four-stream winding tube type heat exchanger III and then is connected with the downstream;

A heavy oil pipeline II at the bottom of the stripping tower, which is used for outputting heavy oil II obtained after the first crude oil is stripped, is sequentially connected with a second tube pass of the double-flow winding tube type heat exchanger V and a first tube pass of the three-flow winding tube type heat exchanger IV and then is connected with the downstream;

A heavy oil pipeline III at the bottom of the stripping tower, which is used for outputting heavy oil III obtained after the first crude oil is stripped, is connected with a third tube pass of the IV third stream winding tube type heat exchanger and then is connected with the downstream;

a heavy oil pipeline IV for outputting heavy oil IV obtained after the first crude oil is stripped at the bottom of the stripping tower is sequentially connected with a second tube pass of a VII double-flow winding tube type heat exchanger and a first tube pass of a VI triple-flow winding tube type heat exchanger and then connected with the downstream;

a first slag reducing pipeline at the bottom of the vacuum tower is sequentially connected with a second tube pass of the four-stream winding tube type heat exchanger III and then connected with the downstream; the second slag reducing pipeline is sequentially connected with the first tube pass of the double-flow winding tube heat exchanger V and the second tube pass of the three-flow winding tube heat exchanger IV and then connected with the downstream;

A first decompression pipeline at the side part of the decompression tower is connected with a third tube pass of the four-flow winding tube type heat exchanger I and then connected with the downstream;

A second decompression pipeline at the side part of the decompression tower is connected with the fourth tube pass of the four-flow winding tube type heat exchanger III and then connected with the downstream;

a third decompression pipeline at the side part of the decompression tower is sequentially connected with a third tube pass of the three-flow winding tube type heat exchanger IV and a third tube pass of the four-flow winding tube type heat exchanger III and then connected with the downstream;

meanwhile, a mixed wax oil pipeline after the connection of the second decompression pipeline and the third decompression pipeline at the side part of the decompression tower is connected with the first tube pass of the double-flow winding tube type heat exchanger II and then connected with the downstream;

The third side line, the first circulating pipeline and the second circulating pipeline of the atmospheric tower are connected with the first decompression pipeline at the side part of the decompression tower, and the mixed diesel pipeline is sequentially connected with the second tube pass of the IV third-stream winding tube type heat exchanger, the second tube pass of the double-stream winding tube type heat exchanger II and the first tube pass of the four-stream winding tube type heat exchanger I and then connected with the downstream.

Preferably, the V-th single-flow heat exchanger is a single-flow winding tube type heat exchanger or a plate type heat exchanger or a common tube type heat exchanger.

In each of the above aspects, the first crude oil is a paraffinic crude oil; the second crude oil is cycloalkyl crude oil.

The invention solves the second technical problem by adopting the technical proposal that: the heat exchange process for exchanging heat by adopting the atmospheric and vacuum heat exchange system is characterized by comprising the following steps:

The first crude oil with the temperature of 20-40 ℃ is input into a first heat exchanger group for heat exchange, the temperature of the first crude oil output from the tail end of the first heat exchanger group is 125-145 ℃, and then the first crude oil enters a first electric desalting device for removing salt and water in the first crude oil; the temperature of the first crude oil after the first electric desalting device is 120-140 ℃, the first crude oil after the first electric desalting device is input into a second heat exchanger group for heat exchange, the temperature of the first crude oil after the first crude oil is taken out is 225-245 ℃ output by the tail end of the second heat exchanger group, and then the first crude oil after the first crude oil is taken out is input into a first primary distillation tower for prefractionation; extracting first primary bottom oil with the temperature of 215-235 ℃ from the bottom of a first primary distillation tower, inputting the first primary bottom oil into a third heat exchanger group for heat exchange, and sequentially conveying the first primary bottom oil with the temperature of 285-305 ℃ output by the tail end of the third heat exchanger group to an atmospheric tower and a vacuum tower to complete atmospheric and vacuum heat exchange;

The second crude oil with the temperature of 20-40 ℃ is input into a fourth heat exchanger group for heat exchange, the temperature of the second crude oil output from the tail end of the fourth heat exchanger group is 125-145 ℃, and then the second crude oil enters a second electric desalting device for removing salt and water in the second crude oil; the temperature of the second crude oil after the second electric desalting device is 120-140 ℃, the second crude oil after the second electric desalting device is input into a fifth heat exchanger group for heat exchange, the temperature of the second crude oil after the second electric desalting device is output from the tail end of the fifth heat exchanger group is 210-235 ℃, and the second crude oil after the second electric desalting device is input into a second primary tower for prefractionation; and extracting second primary bottom oil with the temperature of 200-220 ℃ from the bottom of the second primary distillation tower, inputting the second primary bottom oil into a sixth heat exchanger group for heat exchange, outputting the second primary bottom oil with the temperature of 275-295 ℃ from the tail end of the sixth heat exchanger group, and sequentially conveying the second primary bottom oil to an atmospheric tower and a vacuum tower to complete atmospheric and vacuum heat exchange.

Preferably, the steps specifically include:

The first crude oil with the temperature of 20-40 ℃ is connected into a first pipeline, and enters a shell side of a double-flow winding tubular heat exchanger I to exchange heat with first primary top oil gas with the temperature of 90-110 ℃ from a first top pipeline at the top of a first primary distillation tower and normal top oil gas with the temperature of 95-115 ℃ from a normal top oil gas pipeline of an atmospheric tower to 65-85 ℃, wherein the mass flow ratio of the first crude oil to the first primary top oil gas to the normal top oil gas is 0.75-1.25:0.05-0.25:0.05-0.25; the first crude oil coming out of the shell side of the double-flow winding pipe heat exchanger I enters the shell side of the four-flow winding pipe heat exchanger II and normal top circulating oil with the temperature of 135-155 ℃ from a top circulating pipeline at the top of the atmospheric tower, first primary top circulating oil with the temperature of 135-155 ℃ from a circulating pipeline I at the top of the first primary tower, normal second line oil with the temperature of 155-175 ℃ from a second side line at the upper part of the atmospheric tower, and aviation kerosene product with the temperature of 150-175 ℃ from a second pipe side of the third three-flow winding pipe heat exchanger to exchange heat to 110-135 ℃, wherein the mass flow ratio of the first crude oil to the normal top circulating oil, the first primary top circulating oil, the normal second line oil and the aviation kerosene product is 1:0.7-0.9:0.05-0.25:0.15-0.35:0.15-0.35; the first crude oil coming out of the shell side of the four-stream winding tube heat exchanger II enters a cold medium channel of the single-stream heat exchanger III to exchange heat with vacuum residue at 230-255 ℃ from the third tube side of the four-stream winding tube heat exchanger V to 125-145 ℃, wherein the mass flow ratio between the first crude oil and the vacuum residue is 1:0.05-0.35; the first crude oil coming out of the single-flow heat exchanger III enters a first electric desalting device to remove salt and water in the first crude oil;

The temperature of the first crude oil after the first electric desalting device is 120-140 ℃, the first crude oil enters a shell pass of a three-flow winding tubular heat exchanger IV and normal first medium oil which is from a first circulation pipeline of an atmospheric tower and has the temperature of 210-230 ℃, a second reducing line and second medium oil which are from a second pipeline of a vacuum tower and have the temperature of 230-250 ℃, and a third reducing line which is from a first pipeline of the vacuum tower and has the temperature of 205-225 ℃ are subjected to heat exchange to 185-205 ℃, and the mass flow ratio between the first crude oil after the first crude oil is subjected to the first crude oil, the second reducing line and the second medium oil and the mass flow ratio between the third reducing line and the third reducing line oil are 1:0.45-0.65:0.15-0.35:0.05-0.2; the method comprises the steps that first crude oil after removal, which comes out of a shell pass of a three-stream winding tubular heat exchanger four, enters a shell pass of a four-stream winding tubular heat exchanger five and normal second medium oil which comes from a heat medium channel of a single-stream heat exchanger six and has the temperature of 235-255 ℃, third reduced wire and three medium oil which comes from a second tube pass of a seventh double-stream winding tubular heat exchanger and has the temperature of 235-260 ℃, vacuum residue which comes from a first stream residue reducing pipeline of a vacuum tower and has the temperature of 270-290 ℃, and normal third wire oil which comes from a third side line in the middle of an atmospheric tower and has the temperature of 265-285 ℃ are subjected to heat exchange to 225-245 ℃, wherein the mass flow ratio between the first crude oil after removal and Chang Er medium oil, the third reduced wire and three medium oil, the vacuum residue and the normal third wire oil is 1:0.65-0.85:0.35-0.55:0.05-0.25:0.15-0.35; the crude oil after first removal from the shell side of the four-stream winding tube type heat exchanger five enters a first primary distillation tower for prefractionation;

Extracting first primary bottom oil with the temperature of 215-235 ℃ from the bottom of a first primary distillation tower, and exchanging heat between a cold medium channel of a single-flow heat exchanger six and normal second middle oil with the temperature of 270-290 ℃ from a second circulating pipeline of an atmospheric tower to 245-265 ℃, wherein the mass flow ratio of the first primary bottom oil to the normal second middle oil is 0.8-1.2:0.75-0.95; the first primary bottom oil from the single-flow heat exchanger enters a shell side of a double-flow winding tube heat exchanger seven, exchanges heat with first heavy oil which is from a first heavy oil pipeline of a stripping tower and has the temperature of 335-355 ℃, slag reduction and quenching oil which is from a slag reduction pipeline of a decompression tower and has the temperature of 340-360 ℃ to 285-305 ℃, wherein the mass flow ratio between the first primary bottom oil and the first heavy oil, the slag reduction and quenching oil is 0.8-1.2:0.55-0.75:0.1-0.3;

the first primary bottom oil coming out of the shell side of the double-flow winding tube type heat exchanger seven is sequentially sent to an atmospheric tower and a vacuum tower to complete atmospheric and vacuum heat exchange;

The second crude oil with the temperature of 20-40 ℃ is connected into a second pipeline and enters a shell side of a first single-flow winding tubular heat exchanger to exchange heat with a second primary top oil gas from a second top pipeline at the top of a second primary distillation tower and with the temperature of 85-105 ℃ to 55-75 ℃, wherein the mass flow ratio of the second crude oil to the second primary top oil gas is 0.75-1.25:0.1-0.3; the second crude oil coming out of the shell side of the first single-flow winding pipe heat exchanger enters the shell side of the second double-flow winding pipe heat exchanger to exchange heat with normal top circulating oil which comes from a top circulating pipeline at the top of the atmospheric tower and has the temperature of 115-135 ℃ and first primary top circulating oil which comes from a circulating pipeline at the top of the second primary tower and has the temperature of 135-155 ℃ to 100-120 ℃, wherein the mass flow ratio between the second crude oil and the normal top circulating oil and between the second primary top circulating oil is 0.75-1.25:0.7-0.9:0.25-0.45; the second crude oil coming out of the shell side of the second double-flow winding tubular heat exchanger enters the shell side of the third three-flow winding tubular heat exchanger, and is subjected to heat exchange with first heavy oil which comes from the second tube side of the fifth three-flow winding tubular heat exchanger and has the temperature of 170-190 ℃, aviation kerosene product which comes from the third tube side of the fifth three-flow winding tubular heat exchanger and has the temperature of 175-195 ℃, and normal three-wire oil which comes from the heat medium channel of the fourth single-flow heat exchanger and has the temperature of 155-175 ℃ to 125-145 ℃, wherein the mass flow ratio between the second crude oil and the first heavy oil, the aviation kerosene product and the normal three-wire oil is 0.75-1.25:0.5-0.7:0.1-0.3:0.15-0.35; the second crude oil from the shell side of the third three-stream winding tubular heat exchanger enters a second electric desalting device to remove salt and water in the second crude oil;

The temperature of the second crude oil after the second electric desalting device is 120-140 ℃, and the second crude oil enters a cold medium channel of a fourth single-flow heat exchanger to exchange heat with the normal three-wire oil which is discharged from a fourth tube process of a fourth single-flow winding tube heat exchanger and has the temperature of 210-230 ℃ to 135-155 ℃, wherein the mass flow ratio of the second crude oil after the second crude oil desalting device to the normal three-wire oil is 0.75-1.25:0.15-0.35; the second crude oil after removal from the cooling medium channel of the fourth single-stream heat exchanger enters the shell side of the fifth three-stream winding tube heat exchanger and the normal second-line oil with the temperature of 250-270 ℃ from the second side line at the upper part of the atmospheric tower, the first heavy oil with the temperature of 250-270 ℃ from the first tube side of the seventh double-stream winding tube heat exchanger and the aviation kerosene product with the temperature of 240-260 ℃ from the aviation kerosene hydrogenation device to exchange heat to 220-240 ℃, wherein the mass flow ratio between the second crude oil after removal and the normal second-line oil, the first heavy oil and the aviation kerosene product is 0.75-1.25:0.15-0.35:0.5-0.7:0.1-0.3; the second crude oil after the second removal from the shell side of the fifth three-stream winding pipe heat exchanger enters a cold medium channel of the sixth single-stream heat exchanger and exchanges heat with slag reduction and quenching oil which are from the second pipe side of the double-stream winding pipe heat exchanger and have the temperature of 300-320 ℃ to 210-235 ℃, wherein the mass flow ratio of the crude oil after the second removal to the slag reduction and quenching oil is 0.75-1.25:0.1-0.3; the second crude oil after the removal from the cold medium channel of the sixth single-stream heat exchanger enters a second primary distillation tower for prefractionation;

extracting second primary bottom oil with the temperature of 200-220 ℃ from the bottom of a second primary distillation tower, and enabling the second primary bottom oil to enter a shell side of a seventh double-flow winding pipe type heat exchanger, first heavy oil with the temperature of 295-315 ℃ from a first pipe side of the double-flow winding pipe type heat exchanger seven, a third pipeline with the temperature of 295-315 ℃ from a decompression tower, and three medium oil to exchange heat to 275-295 ℃, wherein the mass flow ratio between the second primary bottom oil and the first heavy oil, the three medium oil and the three medium oil is 0.75-1.25:0.7-0.9:0.5-0.7;

and the second primary bottom oil coming out of the shell side of the seventh double-flow winding tube type heat exchanger is sequentially sent to the atmospheric tower and the vacuum tower to complete atmospheric and vacuum heat exchange.

The technical scheme adopted by the invention for solving the second technical problem can be as follows: the heat exchange process for exchanging heat by adopting the atmospheric and vacuum heat exchange system is characterized by comprising the following steps:

Preferably, the steps specifically include:

The first crude oil with the temperature of 20-40 ℃ is connected into a first pipeline and then divided into two streams, namely first crude oil and second crude oil, wherein the mass flow ratio of the first crude oil to the second crude oil is 1:1; the shell side of the first crude oil entering the single-flow winding tubular heat exchanger I exchanges heat with normal top oil gas pipeline from an atmospheric tower at the temperature of 95-115 ℃ to 70-90 ℃, wherein the mass flow ratio of the first crude oil to the normal top oil gas is 1:0.15-0.35; the second crude oil enters a shell side of a single-flow winding tubular heat exchanger II and exchanges heat with first primary top oil gas which is from a first top pipeline at the top of a first primary distillation tower and has the temperature of 95-115 ℃ to 55-75 ℃, wherein the mass flow ratio of the second crude oil to the first primary top oil gas is 1:0.05-0.25; the first crude oil coming out of the shell side of the single-flow winding pipe heat exchanger I and the single-flow winding pipe heat exchanger II is one-flow, and enters into the shell side of the four-flow winding pipe heat exchanger II and the normal top circulating oil with the temperature of 135-155 ℃ from the top circulating pipeline at the top of the atmospheric tower, the first primary top circulating oil with the temperature of 135-155 ℃ from the circulating pipeline I at the top of the first primary distillation tower, the normal second line oil with the temperature of 155-175 ℃ from the second side line at the upper part of the atmospheric tower and the aviation kerosene product with the temperature of 150-175 ℃ from the second pipe side of the third-flow winding pipe heat exchanger firstly, wherein the mass flow ratio between the first crude oil and the normal top circulating oil, the first primary top circulating oil, the normal second line oil and the aviation kerosene product is 1:0.7-0.9:0.05-0.25:0.15-0.35:0.15-0.35; the first crude oil coming out of the shell side of the four-stream winding tube heat exchanger II enters a cold medium channel of the single-stream heat exchanger III to exchange heat with vacuum residue at 230-255 ℃ from the third tube side of the four-stream winding tube heat exchanger V to 125-145 ℃, wherein the mass flow ratio between the first crude oil and the vacuum residue is 1:0.05-0.35; the first crude oil coming out of the single-flow heat exchanger III enters a first electric desalting device to remove salt and water in the first crude oil;

The first crude oil with the temperature of 30-50 ℃ is input into a first heat exchanger group for heat exchange, the temperature of the first crude oil output from the tail end of the first heat exchanger group is 125-145 ℃, and then the first crude oil enters a first electric desalting device for removing salt and water in the first crude oil; the temperature of the first crude oil after the first electric desalting device is 125-145 ℃, the first crude oil after the first electric desalting device is input into a second heat exchanger group for heat exchange, the temperature of the first crude oil after the first crude oil is removed is 220-240 ℃ output from the tail end of the second heat exchanger group, and the first crude oil after the first crude oil is removed enters a first space of a primary distillation tower for prefractionation; extracting first primary bottom oil with the temperature of 220-240 ℃ from the bottom of a first space of a primary distillation tower, inputting the first primary bottom oil into a third heat exchanger group for heat exchange, outputting the first primary bottom oil with the temperature of 290-310 ℃ from the tail end of the third heat exchanger group, and sequentially conveying the first primary bottom oil to an atmospheric tower and a vacuum tower to complete atmospheric and vacuum heat exchange;

The second crude oil with the temperature of 30-50 ℃ is input into a fourth heat exchanger group for heat exchange, the temperature of the second crude oil output from the tail end of the fourth heat exchanger group is 125-150 ℃, and then the second crude oil enters a second electric desalting device for removing salt and water in the second crude oil; the temperature of the second crude oil after the second electric desalting device is 120-140 ℃, the second crude oil after the second electric desalting device is input into a fifth heat exchanger group for heat exchange, the temperature of the second crude oil after the second electric desalting device is output from the tail end of the fifth heat exchanger group is 200-230 ℃, and the second crude oil after the second electric desalting device is input into a second space of a primary distillation tower for prefractionation; and extracting second primary bottom oil with the temperature of 200-230 ℃ from the bottom of a second space of the primary distillation tower, inputting the second primary bottom oil into a sixth heat exchanger group for heat exchange, outputting the second primary bottom oil with the temperature of 290-310 ℃ by the tail end of the sixth heat exchanger group, and sequentially conveying the second primary bottom oil to an atmospheric tower and a vacuum tower to complete atmospheric and vacuum heat exchange.

Preferably, the steps specifically include:

The first crude oil with the temperature of 30-50 ℃ is connected into a first pipeline and enters a shell side of a four-stream winding tubular heat exchanger I and mixed diesel oil with the temperature of 120-140 ℃ from a second tube side of a double-stream winding tubular heat exchanger II, a aviation kerosene product with the temperature of 140-160 ℃ in a third tube side of the winding tubular heat exchanger, first pressure reducing oil with the temperature of 120-140 ℃ in a pressure reducing pipeline at the side of a pressure reducing tower, first normal top circulating oil with the temperature of 110-130 ℃ in a top circulating pipeline at the top of the atmospheric tower, and heat exchange to 105-125 ℃, wherein the mass flow ratio of the first crude oil to the mixed diesel oil, the aviation kerosene product, the first normal top circulating oil is 0.75-1.25:0.35-0.65:0.05-0.25:0.2-0.5:0.3-0.6; the first crude oil coming out of the shell pass of the four-strand winding tubular heat exchanger I enters the shell pass of the double-strand winding tubular heat exchanger II to exchange heat with mixed wax oil which is from a mixed wax oil pipeline and has the temperature of 180-190 ℃ and mixed diesel oil which is from the second tube pass of the IV three-strand winding tubular heat exchanger and has the temperature of 140-160 ℃ to 125-145 ℃, wherein the mass flow ratio between the first crude oil and the mixed wax oil is 0.75-1.25:0.1-0.4:0.35-0.65; the first crude oil coming out of the shell side of the double-flow winding tubular heat exchanger II enters a first electric desalting device to remove salt and water in the first crude oil;

The temperature of the first crude oil after the first electric desalting device is 125-145 ℃, and the crude oil enters a shell side of a four-strand winding tubular heat exchanger III and a heavy oil pipeline I from a stripping tower, the heavy oil I is at 235-260 ℃, vacuum residue I is from a first residue reduction pipeline of a vacuum tower, the temperature is 235-255 ℃, three-wire oil is from a third pipeline of a three-strand winding tubular heat exchanger IV, the temperature is 235-255 ℃, and two-wire oil is from a second vacuum pipeline of the vacuum tower, the temperature is 235-255 ℃ for heat exchange to 220-240 ℃, wherein the mass flow ratio between the first crude oil after the first crude oil and the heavy oil I, the mass flow ratio between the three-wire oil and the two-wire oil is 0.75-1.25:0.2-0.5:0.1-0.4:0.3-0.6:0.15-0.45; the crude oil after first removal from the shell side of the four-stream winding tube type heat exchanger III enters a first space of a primary distillation tower for prefractionation;

Extracting first primary bottom oil with the temperature of 220-240 ℃ from the bottom of a first space of a primary distillation tower, and enabling the first primary bottom oil to enter a shell side of a three-stream winding tubular heat exchanger IV, heavy oil II with the temperature of 280-300 ℃ from a second tube side of a double-stream winding tubular heat exchanger V, vacuum residue II with the temperature of 280-300 ℃ from the first tube side of the double-stream winding tubular heat exchanger V, and three-wire-reduced oil with the temperature of 280-300 ℃ from a third vacuum pipeline of the vacuum tower, wherein the mass flow ratio between the first primary bottom oil and the heavy oil II, the vacuum residue II and the three-wire-reduced oil is 0.75-1.25:0.05-0.25:0.15-0.45:0.35-0.65; the first primary bottom oil coming out of the shell pass of the three-stream winding tube heat exchanger IV enters the shell pass of the double-stream winding tube heat exchanger V to exchange heat with vacuum residue II from a second residue reduction pipeline of a vacuum tower at the temperature of 350-370 ℃ and heavy oil II from a heavy oil pipeline II of a stripping tower at the temperature of 340-365 ℃ to 290-310 ℃, wherein the mass flow ratio between the first primary bottom oil and the vacuum residue II and between the first primary bottom oil and the vacuum residue II are 0.75-1.25:0.15-0.45:0.02-0.25;

the first primary bottom oil coming out of the shell side of the double-flow winding tubular heat exchanger V is sequentially sent to an atmospheric tower and a vacuum tower to complete atmospheric and vacuum heat exchange;

The second crude oil with the temperature of 30-50 ℃ is connected into a second pipeline, enters the shell side of the I single-flow winding tubular heat exchanger and exchanges heat with normal top oil gas pipeline from the atmospheric tower and normal top oil gas with the temperature of 90-110 ℃ to 60-80 ℃, wherein the mass flow ratio of the second crude oil to the normal top oil gas is 0.75-1.25:0.1-0.4; the second crude oil coming out from the shell side of the I single-flow winding tube heat exchanger enters the shell side of the II single-flow winding tube heat exchanger to exchange heat with primary top oil gas which comes from the top pipeline of the primary distillation tower and has the temperature of 100-120 ℃ to 80-105 ℃, wherein the mass flow ratio between the second crude oil and the primary top oil gas is 0.75-1.25:0.05-0.35; the second crude oil coming out from the shell side of the II single-flow winding tube heat exchanger enters the shell side of the III double-flow winding tube heat exchanger to exchange heat with primary top circulating oil which comes from a circulating pipeline of a primary distillation tower and has the temperature of 145-165 ℃ and normal top circulating oil which comes from a top circulating pipeline of an atmospheric tower and has the temperature of 140-160 ℃ to 125-150 ℃, wherein the mass flow ratio between the second crude oil and the primary top circulating oil and the normal top circulating oil is 0.75-1.25:0.15-0.45:0.6-0.9; the second crude oil coming out from the shell side of the III double-flow winding tubular heat exchanger enters a second electric desalting device to remove salt and water in the second crude oil;

The temperature of the second crude oil after the second electric desalting device is 120-140 ℃ and is divided into two streams, the mass flow ratio of the first stream to the second stream is 0.75:0.25, the first stream enters the shell side of a third stream winding tubular heat exchanger and exchanges heat with aviation kerosene product which is from an aviation kerosene hydrogenation device and has the temperature of 240-260 ℃, mixed diesel oil which is from a mixed diesel oil pipeline and has the temperature of 240-260 ℃, heavy oil which is from a heavy oil pipeline III of a stripping tower and has the temperature of 235-255 ℃ to 215-235 ℃, wherein the mass flow ratio between the second crude oil after the first stream and the aviation kerosene product, the mixed diesel oil and the heavy oil III is 0.75-1.25:0.05-0.35:0.4-0.7:0.15-0.45; the second stream enters a cold medium channel of a V single-stream heat exchanger and exchanges heat with normal-medium oil which is from a first circulating pipeline of an atmospheric tower and has the temperature of 210-230 ℃ to 190-210 ℃, wherein the mass flow ratio between the second crude oil after the second removal in the second stream and the normal-medium oil is 0.75-1.25:1.85-2.15; combining the second crude oil after removal from the shell side of the IV third-stream winding tube type heat exchanger and the cold medium channel of the V single-stream heat exchanger into one stream, and entering a second space of the primary distillation tower for prefractionation;

Withdrawing second primary bottom oil with the temperature of 200-230 ℃ from the bottom of a second space of the primary distillation tower, wherein the second primary bottom oil enters a shell side of a third-strand flow winding tubular heat exchanger VI and exchanges heat with heavy oil IV with the temperature of 280-300 ℃ from a second tube side of a double-strand flow winding tubular heat exchanger VII, normal three-strand oil with the temperature of 280-300 ℃ from a first tube side of the double-strand flow winding tubular heat exchanger VII and normal two-strand oil with the temperature of 280-300 ℃ from a second circulating pipeline of the normal pressure tower, and the normal two-strand oil with the temperature of 280-300 ℃ to 270-290 ℃, wherein the mass flow ratio between the second primary bottom oil and the heavy oil IV, the normal three-strand oil and the normal two-strand oil is 0.75-1.25:0.35-0.65:0.05-0.35:0.75-1.05; the second primary bottom oil coming out from the shell side of the VI three-stream winding tube heat exchanger enters the shell side of the VII double-stream winding tube heat exchanger to exchange heat with normal three-line oil with the temperature of 310-330 ℃ from the third side line of the atmospheric tower and heavy oil with the temperature of 315-335 ℃ from the heavy oil line IV of the stripping tower to 290-310 ℃, wherein the mass flow ratio between the second primary bottom oil and the normal three-line oil as well as the heavy oil IV is 0.75-1.25:0.05-0.35:0.35-0.65;

And (3) sequentially conveying the second primary bottom oil from the shell side of the VII double-flow winding tubular heat exchanger to the atmospheric tower and the vacuum tower to complete atmospheric and vacuum heat exchange.

Compared with the prior art, the application has the advantages that: the oil from the first primary distillation tower or/and the second primary distillation tower or/and the atmospheric tower or/and the vacuum tower or/and the stripping tower in the heat exchange system exchanges heat with each heat exchanger group according to the required working condition, so that the application can treat two different crude oils simultaneously, and the heat loss in the heat exchange process is small; meanwhile, the application utilizes six groups of heat exchanger groups to realize heat exchange of two crude oils, so that a heat exchange network is greatly simplified, and the purposes of reducing investment of equipment, civil engineering, piping and the like, saving energy and reducing consumption are achieved.

Drawings

FIG. 1 is a schematic diagram of an atmospheric and vacuum heat exchange system for crude oil prior to paraffin removal in accordance with an embodiment of the present invention;

FIG. 2 is a schematic diagram of an atmospheric and vacuum heat exchange system for crude oil prior to dealkylation in accordance with an embodiment of the present invention;

FIG. 3 is a schematic diagram of an atmospheric and vacuum heat exchange system for crude oil prior to paraffin removal in accordance with a second embodiment of the present invention;

FIG. 4 is a schematic diagram of an atmospheric and vacuum heat exchange system for crude oil prior to dealkylation in accordance with an embodiment of the present invention;

FIG. 5 is a schematic diagram of an atmospheric and vacuum heat exchange system for crude oil prior to paraffin removal in accordance with a third embodiment of the present invention;

FIG. 6 is a schematic diagram of an atmospheric and vacuum heat exchange system for crude oil prior to a three cycle alkyl de-alkylation in accordance with an embodiment of the present invention;

FIG. 7 is a schematic diagram of a primary distillation tower according to a third 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:

as shown in fig. 1 and 2, a first preferred embodiment of an atmospheric and vacuum heat exchange system with a coiled tube heat exchanger according to the present invention includes a first heat exchanger group E1 for performing primary heat exchange on a first crude oil; a first electric desalting device 1 connected with a first crude oil output end at the tail end of the first heat exchanger group; a second heat exchanger group E2 connected with the output end of the first electric desalting device 1 and used for carrying out secondary heat exchange on the first desalted crude oil obtained after desalting; the first primary distillation tower 2 is connected with the first crude oil output end after the first stripping at the tail end of the second heat exchanger group E2; a third heat exchanger group E3 connected with the bottom of the first primary distillation tower 2 and used for carrying out three heat exchanges on the first primary bottom oil obtained after the primary distillation of the crude oil after the first removal; a stripping tower 9, an atmospheric tower 3 and a vacuum tower 4 which are sequentially connected with the first primary bottom oil output end at the tail end of the third heat exchanger group; a fourth heat exchanger group E4 for performing primary heat exchange on the second crude oil; a second electric desalting device 5 connected with the second crude oil output end at the tail end of the fourth heat exchanger group; a fifth heat exchanger group E5 connected with the output end of the second electric desalting device 5 and used for carrying out secondary heat exchange on the second crude oil after desalting; a second primary distillation tower 6 connected with the second crude oil output end after the removal at the tail end of the fifth heat exchanger group; a sixth heat exchanger group E6 connected with the bottom of the second primary distillation tower 6 and used for carrying out tertiary heat exchange on the second primary bottom oil obtained after the primary distillation of the second crude oil after the removal; the oil from the first primary distillation tower 2 or/and the atmospheric tower 3 or/and the vacuum tower 4 or/and the stripping tower 9 is connected with the first heat exchanger group E1, the second heat exchanger group E2 and the third heat exchanger group E3 according to the required working conditions so as to heat the first crude oil, the first crude oil after the first separation and the first primary bottom oil; the second primary bottom oil output end at the tail end of the sixth heat exchanger group is sequentially connected with the atmospheric tower 3 and the vacuum tower 4, and the oil content from the first primary tower 2 or/and the second primary tower 6 or/and the atmospheric tower 3 or/and the vacuum tower 4 is connected with the fourth heat exchanger group E4, the fifth heat exchanger group E5 and the sixth heat exchanger group E6 according to the required working conditions so as to heat the second crude oil, the second crude oil after the second removal and the second primary bottom oil; at least part of the heat exchangers in the first heat exchanger group E1 or/and the second heat exchanger group E2 or/and the third heat exchanger group E3 are wound tube heat exchangers; at least part of the heat exchangers in the fourth heat exchanger group E4 or/and the fifth heat exchanger group E5 or/and the sixth heat exchanger group 6 are wound tube heat exchangers. The winding tube type heat exchanger is at least one of a single-flow winding tube type heat exchanger, a double-flow winding tube type heat exchanger, a three-flow winding tube type heat exchanger and a four-flow winding tube type heat exchanger, wherein the single-flow winding tube type heat exchanger is a heat exchanger with one shell side and one tube side, the double-flow winding tube type heat exchanger is a heat exchanger with one shell side and two tube sides, the three-flow winding tube type heat exchanger is a heat exchanger with one shell side and three tube sides, and the four-flow winding tube type heat exchanger is a heat exchanger with one shell side and four tube sides. The devices are connected through pipelines.

In this embodiment, the first heat exchanger group E1 includes a double-flow winding tube type heat exchanger one E101, a four-flow winding tube type heat exchanger two E102 and a single-flow heat exchanger three E103, where the single-flow heat exchanger three E103 is a heat exchanger having one heat medium channel and one cold medium channel;

The second heat exchanger group E2 comprises a four-E104 four-stream winding tubular heat exchanger and a five-E105 four-stream winding tubular heat exchanger;

The third heat exchanger group E3 comprises a single-flow heat exchanger six E106 and a double-flow winding tube heat exchanger seven E107, wherein the single-flow heat exchanger six E106 is a heat exchanger with one heat medium channel and one cold medium channel;

The fourth heat exchanger group E4 includes a first single-flow wound tube heat exchanger E201, a second double-flow wound tube heat exchanger E202, and a third triple-flow wound tube heat exchanger E203;

The fifth heat exchanger group E5 includes a fourth single-flow heat exchanger E204, a fifth three-flow wound tube heat exchanger E205, and a sixth single-flow heat exchanger E206, the fourth single-flow heat exchanger E204 being a heat exchanger having one heat medium passage and one cold medium passage, the sixth single-flow heat exchanger E206 being a heat exchanger having one heat medium passage and one cold medium passage;

The sixth heat exchanger group E6 includes a seventh double-flow wound tube heat exchanger E207;

The three E103 single-flow heat exchanger is a single-flow winding tube type heat exchanger or a plate type heat exchanger or a common tube type heat exchanger; the six E106 of the single-flow heat exchanger is a single-flow winding tube type heat exchanger or a plate type heat exchanger or a common tubular heat exchanger; the fourth single-flow heat exchanger E204 is a single-flow winding tube heat exchanger or a plate heat exchanger or a common tube-type heat exchanger; the sixth single-flow heat exchanger E206 is a single-flow wound tube heat exchanger or a plate heat exchanger or a common tube heat exchanger.

The first pipeline A1 for accessing the first crude oil is sequentially connected with a shell side of a double-flow winding tube heat exchanger I101, a shell side of a four-flow winding tube heat exchanger II E102 and a cold medium channel of a single-flow heat exchanger III E103, and then is connected with the first electric desalting device 1; the pipeline of the first electric desalting device 1 is sequentially connected with the shell side of a three-stream winding tubular heat exchanger four E104 and the shell side of a four-stream winding tubular heat exchanger five E105, then is connected with a first primary distillation tower 2, a first pipeline B1 which is used for conveying first primary base oil and comes out of the bottom of the first primary distillation tower 2 is sequentially connected with a cold medium channel of a single-stream heat exchanger six E106 and the shell side of a double-stream winding tubular heat exchanger seven E107, then is connected with a stripping tower 9, and the top output end of the stripping tower 9 is sequentially connected with an atmospheric tower 3 and a vacuum tower 4;

The second pipeline A2 for accessing the second crude oil is sequentially connected with the shell side of the first single-flow winding tubular heat exchanger E201, the shell side of the second double-flow winding tubular heat exchanger E202 and the shell side of the third three-flow winding tubular heat exchanger E203, and then is connected with the second electric desalting device 5; the pipeline of the second electric desalting device 5 is sequentially connected with a cold medium channel of a fourth single-flow heat exchanger E204, a shell side of a fifth three-flow winding tubular heat exchanger E205 and a cold medium channel of a sixth single-flow heat exchanger E206, then is connected with a second primary distillation tower 6, and a second pipeline B2 which is used for conveying second primary base oil and comes out of the bottom of the second primary distillation tower 6 is connected with the shell side of a seventh two-flow winding tubular heat exchanger E207, and then is sequentially connected with the atmospheric tower 3 and the vacuum tower 4;

A first top pipeline 21 at the top of the first primary distillation tower 2 is connected with the first tube pass of the double-flow winding tube type heat exchanger E101 and then connected with the downstream; the first circulating pipeline 22 at the top of the first primary distillation tower 2 is connected with the second tube pass of the four-stream winding tube type heat exchanger II E102 and returns to the first primary distillation tower 2;

A second top pipeline 61 at the top of the second primary distillation tower 6 is connected with the tube pass of the first single-flow winding tube type heat exchanger E201 and then connected with the downstream; a second circulating pipeline 62 at the top of the second primary distillation tower 6 is connected with the second tube pass of the second double-flow winding tube type heat exchanger E202 and returns to the second primary distillation tower 6;

The top circulation pipeline 31 at the top of the atmospheric tower 3 is sequentially connected with the first tube pass of the four-strand winding tube type heat exchanger II 102 and the first tube pass of the second double-strand winding tube type heat exchanger E202 and returns to the atmospheric tower 3;

the normal top oil gas pipeline 32 at the top of the atmospheric tower 3 is connected with the second tube pass of the double-flow winding tube type heat exchanger E101 and then connected with the downstream;

The first pipeline 33 at the top of the atmospheric tower 3 is sequentially connected with a aviation kerosene hydrogenation device, a third tube side of a fifth three-stream winding tube heat exchanger E205, a second tube side of the third three-stream winding tube heat exchanger E203 and a fourth tube side of a four-stream winding tube heat exchanger E102 and then returns to the aviation kerosene hydrogenation device;

The second side line 34 at the upper part of the atmospheric tower 3 is sequentially connected with the first tube pass of the fifth three-stream winding tube heat exchanger E205 and the third tube pass of the fourth-stream winding tube heat exchanger E102 and then connected with the downstream;

The third side line 35 in the middle of the atmospheric tower 3 is sequentially connected with the fourth tube pass of the four-stream winding tube type heat exchanger five E105, the heat medium channel of the fourth single-stream heat exchanger E204 and the third tube pass of the third three-stream winding tube type heat exchanger E203 and then connected with the downstream;

The first circulating pipeline 36 of the atmospheric tower 3 is sequentially connected with the first tube pass of the four E104 of the three-stream winding tube type heat exchanger and returns to the atmospheric tower 3;

the second circulation pipeline 37 of the atmospheric tower 3 is sequentially connected with the heat medium channel of the single-flow heat exchanger six E106 and the first tube pass of the four-flow winding tube heat exchanger five E105 and returns to the atmospheric tower 3;

A first heavy oil pipeline 38 at the bottom of the stripping tower 9 for outputting first heavy oil obtained after the first crude oil stripping is sequentially connected with a first tube side of a double-flow winding tube heat exchanger E107, a first tube side of a seventh double-flow winding tube heat exchanger E207, a second tube side of a fifth three-flow winding tube heat exchanger E205 and a first tube side of a third three-flow winding tube heat exchanger E203 and then connected to the downstream;

The slag reducing pipeline 42 at the bottom of the vacuum tower 4 is sequentially connected with the second tube pass of the double-flow winding tube type heat exchanger seven E107 and the heat medium channel of the sixth single-flow heat exchanger E206 and then divided into two strands, namely a first slag reducing pipeline 41 for conveying vacuum residue and a second slag reducing pipeline for conveying quenching oil, wherein the first slag reducing pipeline 41 is sequentially connected with the third tube pass of the four-flow winding tube type heat exchanger five E105 and the heat medium channel of the single-flow heat exchanger three E103 and then connected with the downstream; the second slag reducing pipeline returns to the vacuum tower 4;

The third pipeline 44 in the middle of the vacuum tower 4 is sequentially connected with the second tube pass of the seventh double-flow winding tube type heat exchanger E207 and the second tube pass of the four-flow winding tube type heat exchanger E105 and then divided into two strands, wherein the first strand of third pipeline 43 is connected with the third tube pass of the three-flow winding tube type heat exchanger E104 and then connected with the downstream, and the second strand of third pipeline returns to the vacuum tower 4;

the second pipeline 45 at the upper part of the pressure reducing tower 4 is connected with the second tube pass of the four E104 of the three-flow winding tube type heat exchanger and then is divided into two streams, wherein the first stream of the second pipeline is connected with the downstream, and the second stream of the second pipeline returns to the pressure reducing tower 4.

The heat exchange steps of the atmospheric and vacuum heat exchange system of the embodiment are as follows:

The first crude oil with the temperature of 20-40 ℃ is connected into a first pipeline A1, and enters a shell side of a double-flow winding tubular heat exchanger E101 to exchange heat with first primary top oil gas with the temperature of 90-110 ℃ from a first top pipeline 21 at the top of a first primary distillation tower 2 and normal top oil gas with the temperature of 95-115 ℃ from a normal top oil gas pipeline 32 of an atmospheric tower 3 to 65-85 ℃, wherein the mass flow ratio of the first crude oil to the first primary top oil gas to the normal top oil gas is 0.75-1.25:0.05-0.25:0.05-0.25; the first crude oil coming out of the shell side of the double-flow winding tube type heat exchanger E101 enters the shell side of the four-flow winding tube type heat exchanger E102 and normal top circulating oil with the temperature of 135-155 ℃ from a top circulating pipeline 31 at the top of the atmospheric tower 3, first primary top circulating oil with the temperature of 135-155 ℃ from a circulating pipeline 22 at the top of the first primary tower 2, normal secondary line oil with the temperature of 155-175 ℃ from a second side line 34 at the upper part of the atmospheric tower 3, and aviation kerosene product with the temperature of 150-175 ℃ from a second tube side of the third-flow winding tube type heat exchanger E203 to exchange heat to 110-135 ℃, wherein the mass flow ratio of the first crude oil to the normal top circulating oil, the first primary top circulating oil, the normal secondary line oil and the aviation kerosene product is 1:0.7-0.9:0.05-0.25:0.15-0.35:0.15-0.35; the first crude oil coming out of the shell side of the four-stream winding tube type heat exchanger II E102 enters a cold medium channel of the single-stream heat exchanger III E103 to exchange heat with vacuum residue with the temperature of 230-255 ℃ from the third tube side of the four-stream winding tube type heat exchanger V E105 to 125-145 ℃, wherein the mass flow ratio between the first crude oil and the vacuum residue is 1:0.05-0.35; the first crude oil coming out of the single-flow heat exchanger three E103 enters the first electric desalting device 1 to remove salt and water in the first crude oil;

The temperature of the first crude oil after the first electric desalting device 1 is 120-140 ℃, the first crude oil enters the shell side of a three-stream winding tube type heat exchanger four E104 and normal first medium oil which is from a first circulation pipeline 36 of an atmospheric tower 3 and has the temperature of 210-230 ℃, the second line and the second medium oil which are from a second pipeline 45 of a vacuum tower 4 and have the temperature of 230-250 ℃, the third line and the third line 43 of the vacuum tower 4 and have the temperature of 205-225 ℃ are subjected to heat exchange to 185-205 ℃, and the mass flow ratio between the first crude oil after the first crude oil is separated and the normal first medium oil, the second line and the second medium oil and the third line is 1:0.45-0.65:0.15-0.35:0.05-0.2; the first crude oil after removal from the shell side of the four E104 of the three-stream winding tube type heat exchanger enters the shell side of the five E105 of the four-stream winding tube type heat exchanger and normal second medium oil with the temperature of 235-255 ℃ from the heat medium channel of the six E106 of the single-stream heat exchanger, the third reduced-pressure oil with the temperature of 235-260 ℃ from the second tube side of the E207 of the seventh double-stream winding tube type heat exchanger, the vacuum residue with the temperature of 270-290 ℃ from the first residue reducing pipeline 41 of the vacuum tower 4, and the normal third line oil with the temperature of 265-285 ℃ from the third side 35 of the middle part of the atmospheric tower 3 are subjected to heat exchange to 225-245 ℃, wherein the mass flow ratio between the first crude oil after removal and the Chang Er medium oil, the third reduced-pressure oil, the vacuum residue and the normal oil is 1:0.65-0.85:0.35-0.55:0.05-0.25:0.15-0.35; the first crude oil after the removal from the shell side of the four-stream winding tube type heat exchanger five E105 enters a first primary distillation tower 2 for prefractionation;

Extracting first primary bottom oil with the temperature of 215-235 ℃ from the bottom of a first primary distillation tower 2, wherein the first primary bottom oil is subjected to heat exchange between a cold medium channel of a six E106 single-stream heat exchanger and normal second middle oil with the temperature of 270-290 ℃ from a second circulation pipeline 37 of an atmospheric tower 3 to 245-265 ℃, and the mass flow ratio of the first primary bottom oil to the normal second middle oil is 0.8-1.2:0.75-0.95; the first primary bottom oil from the single-flow heat exchanger six E106 enters the shell side of the double-flow winding tubular heat exchanger seven E107 to exchange heat with first heavy oil which is from the first heavy oil pipeline 38 of the stripping tower 9 and has the temperature of 335-355 ℃, slag reduction and quenching oil which is from the slag reduction pipeline 42 of the decompression tower 4 and has the temperature of 340-360 ℃ to 285-305 ℃, wherein the mass flow ratio between the first primary bottom oil and the first heavy oil, slag reduction and quenching oil is 0.8-1.2:0.55-0.75:0.1-0.3;

The first primary bottom oil coming out of the shell side of the double-flow winding tube type heat exchanger seven E107 is sequentially sent to the atmospheric tower 3 and the vacuum tower 4 to finish atmospheric and vacuum heat exchange;

The second crude oil with the temperature of 20-40 ℃ is connected into a second pipeline A2, enters into a shell side of a first single-flow winding tubular heat exchanger E201 and exchanges heat with a second primary top oil gas with the temperature of 85-105 ℃ from a second top pipeline 61 at the top of a second primary distillation tower 6 to 55-75 ℃, wherein the mass flow ratio of the second crude oil to the second primary top oil gas is 0.75-1.25:0.1-0.3; the second crude oil coming out of the shell side of the first single-flow winding tube heat exchanger E201 enters the shell side of the second double-flow winding tube heat exchanger E202 to exchange heat with normal top circulation oil with the temperature of 115-135 ℃ from a top circulation pipeline 31 at the top of the atmospheric tower 3 and with the second primary top circulation oil with the temperature of 135-155 ℃ from a circulation pipeline two 62 at the top of the second primary distillation tower 6 to 100-120 ℃, wherein the mass flow ratio between the second crude oil and the normal top circulation oil and between the second primary top circulation oil is 0.75-1.25:0.7-0.9:0.25-0.45; the second crude oil coming out of the shell side of the second double-stream winding tube heat exchanger E202 enters the shell side of the third three-stream winding tube heat exchanger E203 to exchange heat to 125-145 ℃ with the first heavy oil with the temperature of 170-190 ℃ coming from the second tube side of the fifth three-stream winding tube heat exchanger E205, the aviation kerosene product with the temperature of 175-195 ℃ coming from the third tube side of the fifth three-stream winding tube heat exchanger E205, and the normal three-line oil with the temperature of 155-175 ℃ coming from the heat medium channel of the fourth single-stream heat exchanger E204, wherein the mass flow ratio between the second crude oil and the first heavy oil, the aviation kerosene product and the normal three-line oil is 0.75-1.25:0.5-0.7:0.1-0.3:0.15-0.35; the second crude oil coming out of the shell side of the third three-stream winding tubular heat exchanger E203 enters a second electric desalting device 5 to remove salt and water in the second crude oil;

The temperature of the second crude oil after the second electric desalting device 5 is 120-140 ℃, and the second crude oil enters a cold medium channel of a fourth single-flow heat exchanger E204 and exchanges heat with the normal three-line oil which is discharged from a fourth tube process of a four-flow winding tube type heat exchanger five E105 and has the temperature of 210-230 ℃ to 135-155 ℃, wherein the mass flow ratio of the second crude oil after the second crude oil is separated to the normal three-line oil is 0.75-1.25:0.15-0.35; the second crude oil after removal from the cooling medium channel of the fourth single-stream heat exchanger E204 enters the shell side of the fifth three-stream winding tube heat exchanger E205 and the normal second-line oil with the temperature of 250-270 ℃ from the second side line 34 at the upper part of the atmospheric tower 3, the first heavy oil with the temperature of 250-270 ℃ from the first tube side of the seventh double-stream winding tube heat exchanger E207 and the aviation kerosene product with the temperature of 240-260 ℃ from the aviation kerosene hydrogenation device to exchange heat to 220-240 ℃, wherein the mass flow ratio between the second crude oil after removal and the normal second-line oil, the first heavy oil and the aviation kerosene product is 0.75-1.25:0.15-0.35:0.5-0.7:0.1-0.3; the second crude oil after the second removal from the shell side of the fifth three-stream winding pipe heat exchanger E205 enters a cold medium channel of the sixth single-stream heat exchanger E206 and exchanges heat with slag reduction and quenching oil which are from the second pipe side of the double-stream winding pipe heat exchanger E107 and have the temperature of 300-320 ℃ to 210-235 ℃, wherein the mass flow ratio of the second crude oil after the second removal to the slag reduction and quenching oil is 0.75-1.25:0.1-0.3; the second crude oil after the removal from the cold medium channel of the sixth single-stream heat exchanger E206 enters a second primary distillation tower 6 for prefractionation;

Extracting second primary bottom oil with the temperature of 200-220 ℃ from the bottom of a second primary distillation tower 6, and enabling the second primary bottom oil to enter a shell side of a seventh double-flow winding tubular heat exchanger E207, heat-exchanging the first heavy oil with the temperature of 295-315 ℃ from a first tube side of the double-flow winding tubular heat exchanger E107, a third pipeline 44 from a pressure reduction tower 4 and a third line with the temperature of 295-315 ℃ and third medium oil to 275-295 ℃, wherein the mass flow ratio between the second primary bottom oil and the first heavy oil, the third line and the third medium oil is 0.75-1.25:0.7-0.9:0.5-0.7;

And the second primary bottom oil coming out of the shell side of the seventh double-flow winding tubular heat exchanger E207 is sequentially sent to the atmospheric tower 3 and the vacuum tower 4 to finish atmospheric and vacuum heat exchange.

The first crude oil in this embodiment is crude oil before paraffin-based removal, the first crude oil after removal from the first electric desalting device 1 is crude oil after paraffin-based removal, the first primary bottom oil from the first primary distillation tower 2 is paraffin-based primary bottom oil, and the first heavy oil is paraffin-based heavy oil; the second crude oil is crude oil before cycloalkyl removal, the second crude oil after cycloalkyl removal from the second electric desalting device 5 is crude oil after cycloalkyl removal, and the second primary bottom oil from the second primary distillation tower 6 is cycloalkyl primary bottom oil.

Embodiment two:

As shown in fig. 3 to 4, a second preferred embodiment of the atmospheric and vacuum heat exchange system with a coiled tube heat exchanger according to the present invention is basically the same as the first preferred embodiment, except that the first single-flow coiled tube heat exchanger E111 and the second single-flow coiled tube heat exchanger E112 are used in the present embodiment to replace the first double-flow coiled tube heat exchanger E101 in the first preferred embodiment, specifically as follows:

The first pipeline A1 for accessing the first crude oil is divided into two parts, and is respectively connected with the shell side of the single-flow winding tubular heat exchanger I111 and the shell side of the single-flow winding tubular heat exchanger II E112, then sequentially connected to the shell side of the four-flow winding tubular heat exchanger II E102 and the cold medium channel of the single-flow heat exchanger III E103, and then connected with the first electric desalting device 1;

Correspondingly, the heat exchange process comprises the following steps: the first crude oil with the temperature of 20-40 ℃ is connected into a first pipeline A1 and then divided into two streams, namely first crude oil and second crude oil, wherein the mass flow ratio of the first crude oil to the second crude oil is 1:1; the shell side of the first crude oil entering the single-flow winding tubular heat exchanger E111 exchanges heat with normal top oil gas pipeline 32 from the atmospheric tower 3 at the temperature of 95-115 ℃ to 70-90 ℃, wherein the mass flow ratio of the first crude oil to the normal top oil gas is 1:0.15-0.35; the shell side of the second crude oil entering the single-flow winding tube type heat exchanger II E112 exchanges heat with a first primary top oil gas which is from a first top pipeline 21 at the top of the first primary distillation tower 2 and has the temperature of 95-115 ℃ to 55-75 ℃, wherein the mass flow ratio of the second crude oil to the first primary top oil gas is 1:0.05-0.25; the first crude oil coming out of the shell side of the single-flow winding tube type heat exchanger one E111 and the single-flow winding tube type heat exchanger two E112 is one, and then enters the shell side of the four-flow winding tube type heat exchanger two E102 for heat exchange, and the subsequent heat exchange process is the same as that of the first embodiment.

Embodiment III:

As shown in fig. 5 to 7, which are a third preferred embodiment of an atmospheric and vacuum heat exchange system with a coiled tube heat exchanger according to the present invention, the atmospheric and vacuum heat exchange system of the present embodiment includes a first heat exchanger group E1 for performing primary heat exchange on a first crude oil; a first electric desalting device 1 connected with a first crude oil output end at the tail end of the first heat exchanger group; a second heat exchanger group E2 connected with the output end of the first electric desalting device 1 and used for carrying out secondary heat exchange on the first desalted crude oil obtained after desalting; a primary distillation tower 7 connected with the first crude oil output end after the first stripping at the tail end of the second heat exchanger group E2; a third heat exchanger group E3 connected with the bottom of the primary distillation tower 7 and used for carrying out tertiary heat exchange on the first primary bottom oil obtained after the primary distillation of the first crude oil; the stripping tower 9, the atmospheric tower 3 and the vacuum tower 4 are sequentially connected with the first primary bottom oil output end at the tail end of the third heat exchanger group, and oil components coming out of the first primary tower 2 or/and the atmospheric tower 3 or/and the vacuum tower 4 or/and the stripping tower 9 are connected with the first heat exchanger group E1, the second heat exchanger group E2 and the third heat exchanger group E3 according to required working conditions so as to heat the first crude oil, the first crude oil after removal and the first primary bottom oil; at least part of the heat exchangers in the first heat exchanger group E1 or/and the second heat exchanger group E2 or/and the third heat exchanger group E3 are wound tube heat exchangers;

A partition plate 71 is vertically arranged in the primary distillation tower 7, the partition plate 71 is arranged at the lower part of the primary distillation tower 7 and divides the space at the lower part of the primary distillation tower 7 into two parts, namely a first space 7a and a second space 7b, the first space and the second space are communicated with the space at the upper part of the primary distillation tower 7, and the first separated crude oil output end at the tail end of the second heat exchanger group E2 is connected to the first space 7a at the lower part of the primary distillation tower 7; the bottom of the first space 7a is connected with the input end of the third heat exchanger group E3;

The system also comprises a fourth heat exchanger group E4 for carrying out primary heat exchange on the second crude oil; a second electric desalting device 5 connected with the second crude oil output end at the tail end of the fourth heat exchanger group; a fifth heat exchanger group E5 connected with the output end of the second electric desalting device 5 and used for carrying out secondary heat exchange on the second crude oil after desalting; the second crude oil output end after the removal at the tail end of the fifth heat exchanger group E5 is connected to a second space 7b at the lower part of the primary distillation tower 7;

The system also comprises a sixth heat exchanger group E6 which is connected with the bottom of the second space 7b of the primary distillation tower 7 and is used for carrying out tertiary heat exchange on second primary bottom oil obtained after the primary distillation of the second crude oil after the removal; the output end of the second primary bottom oil at the tail end of the sixth heat exchanger group is sequentially connected with the atmospheric tower 3 and the vacuum tower 4, and the oil content from the primary distillation tower 7 or/and the atmospheric tower 3 or/and the vacuum tower 4 or/and the stripping tower 9 is connected with the fourth heat exchanger group E4, the fifth heat exchanger group E5 and the sixth heat exchanger group E6 according to the required working conditions so as to heat the second crude oil, the second crude oil after the second separation and the second primary bottom oil; at least part of the heat exchangers in the fourth heat exchanger group E4 or/and the fifth heat exchanger group E5 or/and the sixth heat exchanger group 6 are wound tube heat exchangers. The winding tube type heat exchanger is at least one of a single-flow winding tube type heat exchanger, a double-flow winding tube type heat exchanger, a three-flow winding tube type heat exchanger and a four-flow winding tube type heat exchanger, wherein the single-flow winding tube type heat exchanger is a heat exchanger with one shell side and one tube side, the double-flow winding tube type heat exchanger is a heat exchanger with one shell side and two tube sides, the three-flow winding tube type heat exchanger is a heat exchanger with one shell side and three tube sides, and the four-flow winding tube type heat exchanger is a heat exchanger with one shell side and four tube sides.

In this embodiment, the first heat exchanger group E1 includes a four-stream wound tube heat exchanger I E and a two-stream wound tube heat exchanger II E132;

the second heat exchanger group E2 comprises four-flow winding tube type heat exchangers III E133;

The third heat exchanger group E3 comprises a three-flow winding tube type heat exchanger IV E134 and a double-flow winding tube type heat exchanger VE135;

the fourth heat exchanger group E4 comprises an I single-flow winding tubular heat exchanger E231, an II single-flow winding tubular heat exchanger E232 and a III double-flow winding tubular heat exchanger E233;

The fifth heat exchanger group E5 comprises an IV third-stream winding tube type heat exchanger E234 and a V single-stream heat exchanger E235, wherein the V single-stream heat exchanger E235 is a heat exchanger with one heat medium channel and one cold medium channel; specifically, the V single-flow heat exchanger E235 is a single-flow winding tube heat exchanger or a plate heat exchanger or a common tube heat exchanger;

The sixth heat exchanger group E6 comprises a third VI winding pipe heat exchanger E236 and a VII double winding pipe heat exchanger E237;

The first pipeline A1 for accessing the first crude oil is sequentially connected with the shell side of the four-stream winding tube heat exchanger I E and the shell side of the double-stream winding tube heat exchanger II E132, and then is connected with the first electric desalting device 1; the pipeline of the first electric desalting device 1 is connected with the shell side of a four-stream winding tubular heat exchanger III E133, then is connected with a first space 7a of a primary distillation tower 7, a first pipeline B1 which is used for conveying first primary bottom oil and comes out of the bottom of the first space 7a is sequentially connected with the shell side of a three-stream winding tubular heat exchanger IV E134 and the shell side of a double-stream winding tubular heat exchanger V E, then is connected with a stripping tower 9, and the top output end of the stripping tower 9 is sequentially connected with an atmospheric tower 3 and a vacuum tower 4;

The second pipeline A2 for accessing the second crude oil is sequentially connected with a shell side of the I single-flow winding tubular heat exchanger E231, a shell side of the II single-flow winding tubular heat exchanger E232 and a shell side of the III double-flow winding tubular heat exchanger E233, and then is connected with a second electric desalting device 5; the pipeline from the second electric desalting device 5 is divided into two paths, and is respectively connected with the shell pass of the IV third-stream winding tubular heat exchanger E234 and the cold medium channel of the V single-stream heat exchanger E235, then connected with the second space 7B of the primary distillation tower 7, and a second pipeline B2 which is used for conveying second primary bottom oil and comes out of the bottom of the second space 7B is sequentially connected with the shell pass of the VI third-stream winding tubular heat exchanger E236 and the shell pass of the VII double-stream winding tubular heat exchanger E237, and then sequentially connected with the atmospheric tower 3 and the vacuum tower 4;

A top pipeline 71 at the top of the primary distillation tower 7 is connected with the tube pass of the II single-flow winding tube type heat exchanger E232 and then connected with the downstream; a circulating pipeline 72 at the top of the primary distillation tower 7 is connected with the first tube pass of the III double-flow winding tube heat exchanger E233 and returns to the primary distillation tower 7;

The first 311 of the top circulation pipeline at the top of the atmospheric tower 3 is connected with the fourth tube pass of the four-stream winding tube heat exchanger I E and returns to the atmospheric tower 3;

the second top circulation pipeline 312 at the top of the atmospheric tower 3 is connected with the second tube pass of the III double-flow winding tube heat exchanger E233 and returns to the atmospheric tower 3;

The normal top oil gas pipeline 32 at the top of the atmospheric tower 3 is connected with the tube pass of the I single-flow winding tube type heat exchanger E231 and then connected with the downstream;

the third side line 35 of the atmospheric tower 3 is sequentially connected with the first tube pass of the VII double-flow winding tube heat exchanger E237 and the second tube pass of the VI third-flow winding tube heat exchanger E236 and then connected with the downstream;

The first circulation pipeline 36 of the atmospheric tower 3 is connected with the heat medium channel of the V single-stream heat exchanger E235 and returns to the atmospheric tower 3;

The second circulation pipeline 37 of the atmospheric tower 3 is connected with the third tube pass of the VI third stream winding tube type heat exchanger E236 and returns to the atmospheric tower 3;

The first pipeline 33 at the top of the atmospheric tower 3 is sequentially connected with a aviation kerosene hydrogenation device, a first tube side of the IV third-stream winding tube heat exchanger E234 and a second tube side of the four-stream winding tube heat exchanger I E131 and returns to the aviation kerosene hydrogenation device;

A heavy oil pipeline 381 at the bottom of the stripping tower 9 for outputting heavy oil I obtained after the first crude oil stripping is connected with the first tube pass of the four-stream winding tube type heat exchanger III E133 and then connected with the downstream;

A heavy oil pipeline two 382 at the bottom of the stripping tower 9 for outputting heavy oil two obtained after the first crude oil stripping is sequentially connected with a second tube pass of the double-flow winding tube heat exchanger V E and a first tube pass of the three-flow winding tube heat exchanger IV E134 and then connected with the downstream;

a heavy oil pipeline III 383 at the bottom of the stripping tower 9 for outputting heavy oil III obtained after the first crude oil stripping is connected with a third tube pass of an IV third stream winding tube type heat exchanger E234 and then connected with the downstream;

A heavy oil pipeline IV 384 at the bottom of the stripping tower 9 for outputting heavy oil IV obtained after the first crude oil stripping is sequentially connected with a second tube pass of the VII double-flow winding tube heat exchanger E237 and a first tube pass of the VI triple-flow winding tube heat exchanger E236 and then connected with the downstream;

The first slag reducing pipeline 411 at the bottom of the vacuum tower 4 is sequentially connected with the second tube pass of the four-stream winding tube type heat exchanger III E133 and then connected with the downstream; the second slag reducing pipeline 412 is connected with the first tube side of the double-flow winding tube heat exchanger V E and the second tube side of the three-flow winding tube heat exchanger IV E134 in sequence and then connected with the downstream;

a first decompression pipeline 413 at the side part of the decompression tower 4 is connected with the third tube pass of the four-flow winding tube type heat exchanger I E and then connected with the downstream;

A second decompression pipeline 414 at the side part of the decompression tower 4 is connected with the fourth tube pass of the four-flow winding tube type heat exchanger III E133 and then connected with the downstream;

The third decompression pipeline 415 at the side part of the decompression tower 4 is sequentially connected with the third tube pass of the three-flow winding tube type heat exchanger IV E134 and the third tube pass of the four-flow winding tube type heat exchanger III E133 and then connected with the downstream;

Meanwhile, a mixed wax oil pipeline 416 formed by connecting a second decompression pipeline 414 and a third decompression pipeline 415 at the side part of the decompression tower 4 is connected with the first tube side of the double-flow winding tube type heat exchanger II E132 and then connected with the downstream;

The third side line 35, the first circulation line 36 and the second circulation line 37 of the atmospheric tower 3 are connected with the first pressure reducing line 413 at the side part of the pressure reducing tower 4, and the mixed diesel line 417 is sequentially connected with the second tube side of the third IV stream winding tube heat exchanger E234, the second tube side of the double stream winding tube heat exchanger II E132 and the first tube side of the four stream winding tube heat exchanger I E and then connected downstream.

The heat exchange process adopting the atmospheric and vacuum heat exchange system of the embodiment comprises the following steps:

The first crude oil with the temperature of 30-50 ℃ is connected into a first pipeline A1, and enters a shell side of a four-stream winding tube heat exchanger I E and mixed diesel oil with the temperature of 120-140 ℃ from a second tube side of a double-stream winding tube heat exchanger II E132, aviation kerosene products with the temperature of 140-160 ℃ in a first tube side of a third stream winding tube heat exchanger E234, first pressure reducing oil with the temperature of 120-140 ℃ in a first pressure reducing pipeline 413 at the side of a pressure reducing tower 4, normal top circulating oil I311 at the top of an atmospheric tower 3 and the temperature of 110-130 ℃ for heat exchange to 105-125 ℃, wherein the mass flow ratio of the first crude oil to mixed diesel oil, aviation kerosene products, the first normal top circulating oil I is 0.75-1.25:0.35-0.65:0.05-0.25:0.2-0.5:0.3-0.6; the first crude oil coming out of the shell pass of the four-stream winding tube heat exchanger I E is subjected to heat exchange between 125 and 145 ℃ by the shell pass of the two-stream winding tube heat exchanger II E132, mixed wax oil which comes from a mixed wax oil pipeline 416 and has the temperature of 180 to 190 ℃ and mixed diesel oil which comes from the second tube pass of the IV three-stream winding tube heat exchanger E234 and has the temperature of 140 to 160 ℃, wherein the mass flow ratio between the first crude oil and the mixed wax oil is 0.75 to 1.25:0.1 to 0.4:0.35 to 0.65; the first crude oil coming out of the shell side of the double-flow winding tube type heat exchanger II E132 enters the first electric desalting device 1 to remove salt and water in the first crude oil;

the temperature of the first crude oil after the first electric desalting device 1 is 125-145 ℃, and the crude oil enters a shell side of a four-flow winding tube type heat exchanger III E133 and a heavy oil I with the temperature of 235-260 ℃ from a heavy oil pipeline I381 of a stripping tower 9, a vacuum residue I with the temperature of 235-255 ℃ from a first residue reduction pipeline 411 of a vacuum tower 4, a three-flow winding tube type heat exchanger IV E134, a second vacuum pipeline 414 with the temperature of 235-255 ℃ and a two-wire oil with the temperature of 235-255 ℃ to exchange heat to 220-240 ℃, wherein the mass flow ratio between the first crude oil after the first crude oil and the heavy oil I, the vacuum residue I, the three-wire oil and the two-wire oil is 0.75-1.25:0.2-0.5:0.1-0.4:0.3-0.6:0.15-0.45; the first crude oil after the removal from the shell side of the four-stream winding tube type heat exchanger III E133 enters a first space 7a of a primary distillation tower 7 for prefractionation;

Withdrawing first primary bottom oil with the temperature of 220-240 ℃ from the bottom of a first space 7a of the primary distillation tower 7, and leading the first primary bottom oil to enter a shell side of a three-stream winding tubular heat exchanger IV E134, a heavy oil II with the temperature of 280-300 ℃ from a second tube side of a double-stream winding tubular heat exchanger V E, a vacuum residue II with the temperature of 280-300 ℃ from a first tube side of the double-stream winding tubular heat exchanger V E135, and a three-wire reducing oil with the temperature of 280-300 ℃ from a third vacuum pipeline 415 of the vacuum tower 4, wherein the mass flow ratio between the first primary bottom oil and the heavy oil II, the vacuum residue II and the three-wire reducing oil is 0.75-1.25:0.05-0.25:0.15-0.45:0.35-0.65; the first primary bottom oil coming out of the shell side of the three-stream winding tube type heat exchanger IV E134 enters the shell side of the double-stream winding tube type heat exchanger V E to exchange heat with the second vacuum residue oil which comes from the second slag reduction pipeline 412 of the vacuum tower 4 and has the temperature of 350-370 ℃, the second heavy oil which comes from the heavy oil pipeline 382 of the stripping tower 9 and has the temperature of 340-365 ℃ to 290-310 ℃, wherein the mass flow ratio between the first primary bottom oil and the second vacuum residue oil is 0.75-1.25:0.15-0.45:0.02-0.25;

the first primary bottom oil from the shell side of the double-flow winding tube heat exchanger V E is sequentially sent to the atmospheric tower 3 and the vacuum tower 4 to complete atmospheric and vacuum heat exchange;

The second crude oil with the temperature of 30-50 ℃ is connected into a second pipeline A2, enters the shell side of an I single-flow winding tubular heat exchanger E231 and exchanges heat with normal top oil gas from a normal top oil gas pipeline 32 of an atmospheric tower 3 at the temperature of 90-110 ℃ to 60-80 ℃, wherein the mass flow ratio of the second crude oil to the normal top oil gas is 0.75-1.25:0.1-0.4; the second crude oil coming out of the shell side of the I single-flow winding tube heat exchanger E231 enters the shell side of the II single-flow winding tube heat exchanger E232 to exchange heat with primary top oil gas which comes from a top pipeline 71 of the primary distillation tower 7 and has the temperature of 100-120 ℃ to 80-105 ℃, wherein the mass flow ratio between the second crude oil and the primary top oil gas is 0.75-1.25:0.05-0.35; the second crude oil coming out of the shell side of the II single-flow winding tube heat exchanger E232 enters the shell side of the III double-flow winding tube heat exchanger E233 to exchange heat with primary top-circulating oil with the temperature of 145-165 ℃ from a circulating pipeline 72 of the primary distillation tower 7 and normal top-circulating oil with the temperature of 140-160 ℃ from a top circulating pipeline II 312 of the normal pressure tower 3 to 125-150 ℃, wherein the mass flow ratio between the second crude oil and the primary top-circulating oil and the normal top-circulating oil II is 0.75-1.25:0.15-0.45:0.6-0.9; the second crude oil coming out of the shell side of the III double-flow winding tubular heat exchanger E233 enters a second electric desalting device 5 to remove salt and water in the second crude oil;

The temperature of the second crude oil after the second electric desalting device 5 is 120-140 ℃ and is divided into two streams, the mass flow ratio of the first stream to the second stream is 0.75:0.25, the first stream enters the shell side of a third stream winding tubular heat exchanger E234 of IV and exchanges heat with aviation kerosene products of 240-260 ℃ from an aviation kerosene hydrogenation device, mixed diesel oil of 240-260 ℃ from a mixed diesel oil pipeline 417 and heavy oil of 235-255 ℃ from a heavy oil pipeline 383 of a stripping tower 9 to 215-235 ℃, wherein the mass flow ratio of the second crude oil after the first stream to the aviation kerosene products, the mixed diesel oil and the heavy oil is 0.75-1.25:0.05-0.35:0.4-0.7:0.15-0.45; the second stream enters the cold medium channel of the V single-stream heat exchanger E235 and exchanges heat with normal medium oil with the temperature of 210-230 ℃ from the first circulating pipeline 36 of the atmospheric tower 3 to 190-210 ℃, wherein the mass flow ratio between the second separated crude oil and the normal medium oil in the second stream is 0.75-1.25:1.85-2.15; combining the second separated crude oil from the shell side of the IV third stream winding pipe type heat exchanger E234 and the cold medium channel of the V single stream heat exchanger E235 into one stream, and entering a second space 7b of the primary distillation tower 7 for prefractionation;

Withdrawing second primary bottom oil with the temperature of 200-230 ℃ from the bottom of a second space 7b of the primary distillation tower 7, wherein the second primary bottom oil enters a shell side of a third strand flow winding tubular heat exchanger E236 of VI and exchanges heat with heavy oil IV with the temperature of 280-300 ℃ from a second tube side of a double strand flow winding tubular heat exchanger E237 of VII, normal three-wire oil with the temperature of 280-300 ℃ from a first tube side of the double strand flow winding tubular heat exchanger E237 of VII and normal two-medium oil with the temperature of 280-300 ℃ from a second circulating pipeline 37 of an atmospheric tower 3 to 270-290 ℃, and the mass flow ratio of the second primary bottom oil to the heavy oil IV, the normal three-wire oil and the normal two-medium oil is 0.75-1.25:0.35-0.65:0.05-0.35:0.05-1.05; the second primary bottom oil coming out of the shell side of the VI three-stream winding tube heat exchanger E236 enters the shell side of the VII double-stream winding tube heat exchanger E237, and exchanges heat with normal-temperature three-wire oil with the temperature of 310-330 ℃ from the third side line 35 of the atmospheric tower 3 and heavy oil with the temperature of 315-335 ℃ from the heavy oil line IV 384 of the stripping tower 9 to 290-310 ℃, wherein the mass flow ratio between the second primary bottom oil and the normal-temperature three-wire oil and the heavy oil IV is 0.75-1.25:0.05-0.35:0.35-0.65;

And the second primary bottom oil coming out of the shell side of the VII double-flow winding tubular heat exchanger E237 is sequentially sent to the atmospheric tower 3 and the vacuum tower 4 to finish atmospheric and vacuum heat exchange.

The first crude oil in this embodiment is crude oil before paraffin-based removal, the first crude oil after removal from the first electric desalting device 1 is crude oil after paraffin-based removal, the first primary bottom oil from the first primary distillation tower 2 is paraffin-based primary bottom oil, the heavy oil one is paraffin-based normal slag one, the heavy oil two is paraffin-based normal slag two, the heavy oil three is paraffin-based normal slag three, and the heavy oil four is paraffin-based normal slag four.

The second crude oil is crude oil before cycloalkyl removal, the second crude oil after cycloalkyl removal from the second electric desalting device 5 is crude oil after cycloalkyl removal, and the second primary bottom oil from the second primary distillation tower 6 is cycloalkyl primary bottom oil.

Claims

1. An atmospheric and vacuum heat exchange system with a wound tube heat exchanger includes a first heat exchanger group (E1) for primary heat exchange of a first crude oil; a first electro-desalting device (1) connected with a first crude oil output end at the tail end of the first heat exchanger group; the second heat exchanger group (E2) is connected with the output end of the first electric desalting device (1) and is used for carrying out secondary heat exchange on the first desalted crude oil obtained after desalting; the first primary distillation tower (2) is connected with the first crude oil output end after the first stripping at the tail end of the second heat exchanger group (E2); the third heat exchanger group (E3) is connected with the bottom of the first primary distillation tower (2) and is used for carrying out tertiary heat exchange on the first primary bottom oil obtained after the primary distillation of the crude oil after the first removal; the stripping tower (9), the atmospheric tower (3) and the vacuum tower (4) are sequentially connected with the first primary bottom oil output end at the tail end of the third heat exchanger group, and oil components coming out of the first primary distillation tower (2) or/and the atmospheric tower (3) or/and the vacuum tower (4) or/and the stripping tower (9) are connected with the first heat exchanger group (E1), the second heat exchanger group (E2) and the third heat exchanger group (E3) according to required working conditions so as to heat the first crude oil, the first crude oil after removal and the first primary bottom oil; at least part of heat exchangers in the first heat exchanger group (E1) or/and the second heat exchanger group (E2) or/and the third heat exchanger group (E3) are wound tube heat exchangers;

The method is characterized in that: the system also comprises a fourth heat exchanger group (E4) for carrying out primary heat exchange on the second crude oil; a second electric desalting device (5) connected with the second crude oil output end at the tail end of the fourth heat exchanger group; a fifth heat exchanger group (E5) connected with the output end of the second electric desalting device (5) and used for carrying out secondary heat exchange on the second desalted crude oil obtained after desalting; the second primary distillation tower (6) is connected with the second crude oil output end after the removal at the tail end of the fifth heat exchanger group; a sixth heat exchanger group (E6) connected with the bottom of the second primary distillation tower (6) and used for carrying out tertiary heat exchange on the second primary bottom oil obtained after the primary distillation of the second crude oil after the removal; the second primary bottom oil output end at the tail end of the sixth heat exchanger group is sequentially connected with the atmospheric tower (3) and the vacuum tower (4), and the oil content from the first primary distillation tower (2) or/and the second primary distillation tower (6) or/and the atmospheric tower (3) or/and the vacuum tower (4) is connected with the fourth heat exchanger group (E4), the fifth heat exchanger group (E5) and the sixth heat exchanger group (E6) according to the required working conditions so as to heat the second crude oil, the second removed crude oil and the second primary bottom oil; at least part of heat exchangers in the fourth heat exchanger group (E4) or/and the fifth heat exchanger group (E5) or/and the sixth heat exchanger group (E6) are wound tube heat exchangers.

2. The atmospheric and vacuum heat exchange system of claim 1, wherein: the winding tube type heat exchanger is at least one of a single-flow winding tube type heat exchanger, a double-flow winding tube type heat exchanger, a three-flow winding tube type heat exchanger and a four-flow winding tube type heat exchanger, the single-flow winding tube type heat exchanger is a heat exchanger with one shell side and one tube side, the double-flow winding tube type heat exchanger is a heat exchanger with one shell side and two tube sides, the three-flow winding tube type heat exchanger is a heat exchanger with one shell side and three tube sides, and the four-flow winding tube type heat exchanger is a heat exchanger with one shell side and four tube sides.

3. The atmospheric and vacuum heat exchange system of claim 2, wherein: the first heat exchanger group (E1) comprises a double-flow winding tubular heat exchanger I (E101), a four-flow winding tubular heat exchanger II (E102) and a single-flow heat exchanger III (E103), wherein the single-flow heat exchanger III (E103) is a heat exchanger with one heat medium channel and one cold medium channel;

The second heat exchanger group (E2) comprises a four-stream winding tube type heat exchanger (E104) and a five-stream winding tube type heat exchanger (E105);

the third heat exchanger group (E3) comprises a single-flow heat exchanger six (E106) and a double-flow winding tube heat exchanger seven (E107), wherein the single-flow heat exchanger six (E106) is a heat exchanger with one heat medium channel and one cold medium channel;

the fourth heat exchanger group (E4) comprises a first single-flow winding tube heat exchanger (E201), a second double-flow winding tube heat exchanger (E202) and a third three-flow winding tube heat exchanger (E203);

The fifth heat exchanger group (E5) comprises a fourth single-flow heat exchanger (E204), a fifth three-flow wound tube heat exchanger (E205) and a sixth single-flow heat exchanger (E206), wherein the fourth single-flow heat exchanger (E204) is a heat exchanger with one heat medium channel and one cold medium channel, and the sixth single-flow heat exchanger (E206) is a heat exchanger with one heat medium channel and one cold medium channel;

the sixth heat exchanger group (E6) comprises a seventh double-flow wound tube heat exchanger (E207);

The first pipeline (A1) for accessing the first crude oil is sequentially connected with a shell side of a double-flow winding tubular heat exchanger I (E101), a shell side of a four-flow winding tubular heat exchanger II (E102) and a cold medium channel of a single-flow heat exchanger III (E103), and then is connected with the first electric desalting device (1); the pipeline of the first electric desalting device (1) is sequentially connected with the shell side of a three-stream winding tubular heat exchanger IV (E104) and the shell side of a four-stream winding tubular heat exchanger V (E105), then is connected with a first primary distillation tower (2), a first pipeline (B1) which is used for conveying first primary bottom oil and comes out of the bottom of the first primary distillation tower (2) is sequentially connected with a cold medium channel of a single-stream heat exchanger VI (E106) and the shell side of a double-stream winding tubular heat exchanger V (E107), then is connected with a stripping tower (9), and the top output end of the stripping tower (9) is sequentially connected with the atmospheric tower (3) and a decompression tower (4);

A second pipeline (A2) for accessing second crude oil is sequentially connected with a shell side of the first single-flow winding tubular heat exchanger (E201), a shell side of the second double-flow winding tubular heat exchanger (E202) and a shell side of the third three-flow winding tubular heat exchanger (E203), and then is connected with a second electric desalting device (5); the pipeline of the second electric desalting device (5) is sequentially connected with a cold medium channel of a fourth single-flow heat exchanger (E204), a shell pass of a fifth three-flow winding tubular heat exchanger (E205) and a cold medium channel of a sixth single-flow heat exchanger (E206), then is connected with a second primary tower (6), and a second pipeline (B2) which is used for conveying second primary bottom oil and comes out of the bottom of the second primary tower (6) is connected with a shell pass of a seventh double-flow winding tubular heat exchanger (E207), and then is sequentially connected with the atmospheric tower (3) and the vacuum tower (4);

A first top pipeline (21) at the top of the first primary distillation tower (2) is connected with the first tube pass of the double-flow winding tube type heat exchanger I (E101) and then connected with the downstream; a first circulating pipeline (22) at the top of the first primary distillation tower (2) is connected with a second tube pass of the four-stream winding tube type heat exchanger II (E102) and then returns to the first primary distillation tower (2);

A second top pipeline (61) at the top of the second primary distillation tower (6) is connected with the tube pass of the first single-flow winding tube type heat exchanger (E201) and then connected with the downstream; a circulation pipeline II (62) at the top of the second primary distillation tower (6) is connected with a second tube pass of the second double-flow winding tube type heat exchanger (E202) and then returns to the second primary distillation tower (6);

The top circulation pipeline (31) at the top of the atmospheric tower (3) is sequentially connected with the first tube pass of the four-flow winding tube type heat exchanger II (E102) and the first tube pass of the second double-flow winding tube type heat exchanger (E202) and returns to the atmospheric tower (3);

A normal top oil gas pipeline (32) at the top of the atmospheric tower (3) is connected with the second tube pass of the double-flow winding tube type heat exchanger I (E101) and then connected with the downstream;

A first pipeline (33) at the top of the atmospheric tower (3) is sequentially connected with a aviation kerosene hydrogenation device, a third tube pass of a fifth three-flow winding tube type heat exchanger (E205), a second tube pass of the third three-flow winding tube type heat exchanger (E203) and a fourth tube pass of a four-flow winding tube type heat exchanger (E102) and returns to the aviation kerosene hydrogenation device;

the second side line (34) at the upper part of the atmospheric tower (3) is sequentially connected with the first tube pass of the fifth three-flow winding tube type heat exchanger (E205) and the third tube pass of the fourth-flow winding tube type heat exchanger II (E102) and then connected with the downstream;

The third side line (35) in the middle of the atmospheric tower (3) is sequentially connected with the fourth tube pass of the four-stream winding tube type heat exchanger five (E105), the heat medium channel of the fourth single-stream heat exchanger (E204) and the third tube pass of the third three-stream winding tube type heat exchanger (E203) and then connected with the downstream;

The first circulating pipeline (36) of the atmospheric tower (3) is sequentially connected with the first tube pass of the three-flow winding tube type heat exchanger IV (E104) and then returns to the atmospheric tower (3);

the second circulating pipeline (37) of the atmospheric tower (3) is sequentially connected with a heat medium channel of a single-flow heat exchanger six (E106) and a first tube side of a four-flow winding tube type heat exchanger five (E105) and then returns to the atmospheric tower (3);

A first heavy oil pipeline (38) at the bottom of the stripping tower (9) for outputting first heavy oil obtained after first crude oil stripping is sequentially connected with a first tube side of a double-flow winding tube type heat exchanger seven (E107), a first tube side of a seventh double-flow winding tube type heat exchanger (E207), a second tube side of a fifth three-flow winding tube type heat exchanger (E205) and a first tube side of a third three-flow winding tube type heat exchanger (E203) and then connected to the downstream;

The slag reducing pipeline (42) at the bottom of the vacuum tower (4) is sequentially connected with the second tube pass of the double-flow winding tube type heat exchanger seven (E107) and the heat medium channel of the sixth single-flow heat exchanger (E206) and then divided into two strands, namely a first slag reducing pipeline (41) for conveying vacuum residuum and a second slag reducing pipeline for conveying quenching oil, wherein the first slag reducing pipeline (41) is sequentially connected with the third tube pass of the four-flow winding tube type heat exchanger five (E105) and the heat medium channel of the single-flow heat exchanger three (E103) and then connected with the downstream; the second strand slag reducing pipeline returns to the pressure reducing tower (4);

A third pipeline in the middle of the vacuum tower (4) is sequentially connected with a second tube pass of a seventh double-flow winding tube type heat exchanger (E207) and a second tube pass of a four-flow winding tube type heat exchanger (E105) and then divided into two strands, wherein the first strand of third pipeline is connected with a third tube pass of a four-flow winding tube type heat exchanger (E104) and then connected with the downstream, and the second strand of third pipeline returns to the vacuum tower (4);

A second pipeline (45) at the upper part of the vacuum tower (4) is connected with a second tube pass of the three-flow winding tube type heat exchanger four (E104) and then is divided into two strands, wherein a first strand of second pipeline is connected with the downstream, and a second strand of second pipeline returns to the vacuum tower (4).

4. The atmospheric and vacuum heat exchange system of claim 2, wherein: the first heat exchanger group (E1) comprises a single-flow winding tube type heat exchanger I (E111), a single-flow winding tube type heat exchanger II (E112), a four-flow winding tube type heat exchanger II (E102) and a single-flow heat exchanger III (E103), wherein the single-flow heat exchanger III (E103) is a heat exchanger with one heat medium channel and one cold medium channel;

The first pipeline (A1) for accessing the first crude oil is divided into two parts, and is respectively connected with the shell side of the single-flow winding tubular heat exchanger I (E111) and the shell side of the single-flow winding tubular heat exchanger II (E112) and then is connected with the cold medium channels of the shell side of the four-flow winding tubular heat exchanger II (E102) and the single-flow heat exchanger III (E103) in sequence, and then is connected with the first electric desalting device (1); the pipeline of the first electric desalting device (1) is sequentially connected with the shell side of a three-stream winding tubular heat exchanger IV (E104) and the shell side of a four-stream winding tubular heat exchanger V (E105), then is connected with a first primary distillation tower (2), a first pipeline (B1) which is used for conveying first primary bottom oil and comes out of the bottom of the first primary distillation tower (2) is sequentially connected with a cold medium channel of a single-stream heat exchanger VI (E106) and the shell side of a double-stream winding tubular heat exchanger V (E107), then is connected with a stripping tower (9), and the top output end of the stripping tower (9) is sequentially connected with the atmospheric tower (3) and a decompression tower (4);

a first top pipeline (21) at the top of the first primary distillation tower (2) is connected with the tube pass of the single-flow winding tube type heat exchanger II (E112) and then connected with the downstream; a first circulating pipeline (22) at the top of the first primary distillation tower (2) is connected with a second tube pass of the four-stream winding tube type heat exchanger II (E102) and then returns to the first primary distillation tower (2);

a normal top oil gas pipeline (32) at the top of the atmospheric tower (3) is connected with the tube pass of the single-flow winding tube type heat exchanger I (E111) and then connected with the downstream;

5. The atmospheric and vacuum heat exchange system according to claim 3 or 4, wherein: the third single-flow heat exchanger (E103) is a single-flow winding tube type heat exchanger or a plate type heat exchanger or a common tube type heat exchanger; the six single-flow heat exchanger (E106) is a single-flow winding tube type heat exchanger or a plate type heat exchanger or a common tube type heat exchanger; the fourth single-flow heat exchanger (E204) is a single-flow winding tube type heat exchanger or a plate type heat exchanger or a common tube type heat exchanger; the sixth single-flow heat exchanger (E206) is a single-flow winding tube type heat exchanger or a plate type heat exchanger or a common tube type heat exchanger.

6. An atmospheric and vacuum heat exchange system with a wound tube heat exchanger includes a first heat exchanger group (E1) for primary heat exchange of a first crude oil; a first electro-desalting device (1) connected with a first crude oil output end at the tail end of the first heat exchanger group; the second heat exchanger group (E2) is connected with the output end of the first electric desalting device (1) and is used for carrying out secondary heat exchange on the first desalted crude oil obtained after desalting; a primary distillation tower (7) connected with the output end of the first crude oil after the removal at the tail end of the second heat exchanger group (E2); the third heat exchanger group (E3) is connected with the bottom of the primary distillation tower (7) and is used for carrying out tertiary heat exchange on the first primary bottom oil obtained after the primary distillation of the crude oil after the first removal; the stripping tower (9), the atmospheric tower (3) and the vacuum tower (4) are sequentially connected with the first primary bottom oil output end at the tail end of the third heat exchanger group, and oil components from the primary distillation tower (7) or/and the atmospheric tower (3) or/and the vacuum tower (4) or/and the stripping tower (9) are connected with the first heat exchanger group (E1), the second heat exchanger group (E2) and the third heat exchanger group (E3) according to required working conditions so as to heat the first crude oil, the first crude oil after removal and the first primary bottom oil; at least part of heat exchangers in the first heat exchanger group (E1) or/and the second heat exchanger group (E2) or/and the third heat exchanger group (E3) are wound tube heat exchangers;

The method is characterized in that: a partition board is vertically arranged in the primary distillation tower (7), the partition board is arranged at the lower part of the primary distillation tower (7) and divides the space at the lower part of the primary distillation tower (7) into two parts, namely a first space (7 a) and a second space (7 b), the first space and the second space are communicated with the space at the upper part of the primary distillation tower (7), and a first crude oil output end at the tail end of the second heat exchanger group (E2) is connected to the first space (7 a) at the lower part of the primary distillation tower (7); the bottom of the first space (7 a) is connected with the input end of the third heat exchanger group (E3);

The system also comprises a fourth heat exchanger group (E4) for carrying out primary heat exchange on the second crude oil; a second electric desalting device (5) connected with the second crude oil output end at the tail end of the fourth heat exchanger group; a fifth heat exchanger group (E5) connected with the output end of the second electric desalting device (5) and used for carrying out secondary heat exchange on the second desalted crude oil obtained after desalting; the second crude oil output end after the removal at the tail end of the fifth heat exchanger group (E5) is connected to a second space (7 b) at the lower part of the primary distillation tower (7);

The system also comprises a sixth heat exchanger group (E6) which is connected with the bottom of a second space (7 b) of the primary distillation tower (7) and is used for carrying out tertiary heat exchange on second primary bottom oil obtained after the primary distillation of second crude oil; the second primary bottom oil output end at the tail end of the sixth heat exchanger group is sequentially connected with the atmospheric tower (3) and the vacuum tower (4), and the oil discharged from the primary distillation tower (7) or/and the atmospheric tower (3) or/and the vacuum tower (4) or/and the stripping tower (9) is connected with the fourth heat exchanger group (E4), the fifth heat exchanger group (E5) and the sixth heat exchanger group (E6) according to the required working conditions so as to heat the second crude oil, the second separated crude oil and the second primary bottom oil; at least part of heat exchangers in the fourth heat exchanger group (E4) or/and the fifth heat exchanger group (E5) or/and the sixth heat exchanger group (E6) are wound tube heat exchangers.

7. The atmospheric and vacuum heat exchange system of claim 6, wherein: the winding tube type heat exchanger is at least one of a single-flow winding tube type heat exchanger, a double-flow winding tube type heat exchanger, a three-flow winding tube type heat exchanger and a four-flow winding tube type heat exchanger, the single-flow winding tube type heat exchanger is a heat exchanger with one shell side and one tube side, the double-flow winding tube type heat exchanger is a heat exchanger with one shell side and two tube sides, the three-flow winding tube type heat exchanger is a heat exchanger with one shell side and three tube sides, and the four-flow winding tube type heat exchanger is a heat exchanger with one shell side and four tube sides.

8. The atmospheric and vacuum heat exchange system of claim 7, wherein: the first heat exchanger group (E1) comprises a four-flow winding tube type heat exchanger I (E131) and a double-flow winding tube type heat exchanger II (E132);

the second heat exchanger group (E2) comprises a four-stream wound tube heat exchanger III (E133);

The third heat exchanger group (E3) comprises a three-flow winding tube type heat exchanger IV (E134) and a double-flow winding tube type heat exchanger V (E135);

the fourth heat exchanger group (E4) comprises an I single-flow winding tube heat exchanger (E231), an II single-flow winding tube heat exchanger (E232) and a III double-flow winding tube heat exchanger (E233);

the fifth heat exchanger group (E5) comprises an IV third-stream winding tube type heat exchanger (E234) and a V single-stream heat exchanger (E235), wherein the V single-stream heat exchanger (E235) is a heat exchanger with one heat medium channel and one cold medium channel;

the sixth heat exchanger group (E6) comprises a third VI flow wound tubular heat exchanger (E236) and a VII double flow wound tubular heat exchanger (E237);

The first pipeline (A1) for accessing the first crude oil is sequentially connected with a shell side of the four-stream winding tubular heat exchanger I (E131) and a shell side of the double-stream winding tubular heat exchanger II (E132), and then is connected with the first electric desalting device (1); the pipeline of the first electric desalting device (1) is connected with the shell side of a four-stream winding tubular heat exchanger III (E133), then is connected with a first space (7 a) of a primary distillation tower (7), a first pipeline (B1) which is used for conveying first primary bottom oil and is arranged at the bottom of the first space (7 a) is sequentially connected with the shell side of a three-stream winding tubular heat exchanger IV (E134) and the shell side of a double-stream winding tubular heat exchanger V (E135), then is connected with a stripping tower (9), and the top output end of the stripping tower (9) is sequentially connected with the atmospheric tower (3) and a decompression tower (4);

The second pipeline (A2) for accessing the second crude oil is sequentially connected with a shell side of the I single-flow winding tubular heat exchanger (E231), a shell side of the II single-flow winding tubular heat exchanger (E232) and a shell side of the III double-flow winding tubular heat exchanger (E233), and then is connected with a second electric desalting device (5); the pipeline which is discharged from the second electric desalting device (5) is divided into two paths, and is respectively connected with the shell side of an IV third-stream winding tubular heat exchanger (E234) and the cold medium channel of a V single-stream heat exchanger (E235) and then is connected with a second space (7B) of the primary distillation tower (7), a second pipeline (B2) which is discharged from the bottom of the second space (7B) and is used for conveying second primary bottom oil is sequentially connected with the shell side of a VI third-stream winding tubular heat exchanger (E236) and the shell side of a VII double-stream winding tubular heat exchanger (E237), and then is sequentially connected with the atmospheric tower (3) and the vacuum tower (4);

The top pipeline at the top of the primary distillation tower (7) is connected with the tube pass of the II single-flow winding tube type heat exchanger (E232) and then connected with the downstream; a circulating pipeline (72) at the top of the primary distillation tower (7) is connected with the first tube pass of the III double-flow winding tube type heat exchanger (E233) and then returns to the primary distillation tower (7);

The first top circulating pipeline (311) at the top of the atmospheric tower (3) is connected with the fourth tube pass of the four-flow winding tube type heat exchanger I (E131) and returns to the atmospheric tower (3);

A top circulation pipeline II (312) at the top of the atmospheric tower (3) is connected with a second tube pass of the III double-flow winding tube type heat exchanger (E233) and returns to the atmospheric tower (3);

A normal top oil gas pipeline (32) at the top of the atmospheric tower (3) is connected with the tube pass of the I single-flow winding tube type heat exchanger (E231) and then connected with the downstream;

The third side line (35) of the atmospheric tower (3) is sequentially connected with the first tube pass of the VII double-flow winding tube heat exchanger (E237) and the second tube pass of the VI third-flow winding tube heat exchanger (E236) and then connected with the downstream;

The first circulating pipeline (36) of the atmospheric tower (3) is connected with the heat medium channel of the V single-stream heat exchanger (E235) and returns to the atmospheric tower (3);

The second circulating pipeline (37) of the atmospheric tower (3) is connected with the third tube side of the VI third-stream winding tube type heat exchanger (E236) and returns to the atmospheric tower (3);

A first pipeline (33) at the top of the atmospheric tower (3) is sequentially connected with a aviation kerosene hydrogenation device, a first tube pass of a third IV stream winding tube type heat exchanger (E234) and a second tube pass of a fourth stream winding tube type heat exchanger I (E131) and then returns to the aviation kerosene hydrogenation device;

a heavy oil pipeline I (381) at the bottom of the stripping tower (9) for outputting heavy oil I obtained after the first crude oil stripping is connected with a first tube side of the four-stream winding tube type heat exchanger III (E133) and then connected with the downstream;

a heavy oil pipeline II (382) at the bottom of the stripping tower (9) for outputting heavy oil II obtained after the first crude oil stripping is sequentially connected with a second tube pass of the double-flow winding tube type heat exchanger V (E135) and a first tube pass of the three-flow winding tube type heat exchanger IV (E134) and then connected with the downstream;

A heavy oil pipeline III (383) at the bottom of the stripping tower (9) for outputting heavy oil III obtained after the first crude oil stripping is connected with a third tube side of a third IV stream winding tube type heat exchanger (E234) and then connected with the downstream;

A heavy oil pipeline IV (384) at the bottom of the stripping tower (9) for outputting heavy oil IV obtained after the first crude oil stripping is sequentially connected with a second tube pass of a VII double-flow winding tube heat exchanger (E237) and a first tube pass of a VI third-flow winding tube heat exchanger (E236) and then connected with the downstream;

A first slag reducing pipeline (411) at the bottom of the pressure reducing tower (4) is sequentially connected with the second tube pass of the four-flow winding tube type heat exchanger III (E133) and then connected with the downstream; the second slag reducing pipeline (412) is sequentially connected with the first tube pass of the double-flow winding tube type heat exchanger V (E135) and the second tube pass of the three-flow winding tube type heat exchanger IV (E134) and then connected with the downstream;

a first decompression pipeline (413) at the side part of the decompression tower (4) is connected with the third tube pass of the four-flow winding tube type heat exchanger I (E131) and then connected with the downstream;

A second decompression pipeline (414) at the side part of the decompression tower (4) is connected with the fourth tube pass of the four-flow winding tube type heat exchanger III (E133) and then connected with the downstream;

A third decompression pipeline (415) at the side part of the decompression tower (4) is sequentially connected with a third tube pass of the three-flow winding tube type heat exchanger IV (E134) and a third tube pass of the four-flow winding tube type heat exchanger III (E133) and then connected with the downstream;

Meanwhile, a mixed wax oil pipeline (416) connected by a second decompression pipeline (414) and a third decompression pipeline (415) at the side part of the decompression tower (4) is connected with the first tube side of the double-flow winding tube type heat exchanger II (E132) and then connected with the downstream;

The third side line (35), the first circulating pipeline (36), the second circulating pipeline (37) of the atmospheric tower (3) and the mixed diesel pipeline (417) connected with the first decompression pipeline (413) at the side part of the decompression tower (4) are sequentially connected with the second tube side of the IV third-stream winding tube type heat exchanger (E234), the second tube side of the double-stream winding tube type heat exchanger II (E132) and the first tube side of the four-stream winding tube type heat exchanger I (E131) and then connected with the downstream.

9. The atmospheric and vacuum heat exchange system of claim 8, wherein: the V-th single-flow heat exchanger (E235) is a single-flow winding tube type heat exchanger or a plate type heat exchanger or a common tube type heat exchanger.

10. The atmospheric and vacuum heat exchange system according to any one of claims 1 to 4,6 to 9, wherein: the first crude oil is paraffin-based crude oil; the second crude oil is cycloalkyl crude oil.