CN112442389B

CN112442389B - Wax oil hydrocracking device

Info

Publication number: CN112442389B
Application number: CN201910833235.1A
Authority: CN
Inventors: 朱赫礼; 桑守余; 吴闯; 严岩; 刘小波; 赵秀文
Original assignee: Petrochina Co Ltd
Current assignee: Petrochina Co Ltd
Priority date: 2019-09-04
Filing date: 2019-09-04
Publication date: 2022-10-04
Anticipated expiration: 2039-09-04
Also published as: CN112442389A

Abstract

The invention provides a wax oil hydrocracking device, which comprises: the material storage tank assembly is used for storing raw materials; a diesel side line tower for producing diesel; the diesel tower bottom reboiling furnace is communicated with the diesel side tower and is used for exchanging heat with the diesel; the diesel oil heat exchange pipeline is provided with a diesel oil inlet and a diesel oil outlet, the diesel oil inlet is communicated with an outlet of the diesel oil side line tower, and the diesel oil outlet is communicated with an inlet of the reboiling furnace at the bottom of the diesel oil tower; the first heat exchanger is arranged on a diesel oil heat exchange pipeline, a raw material inlet of the first heat exchanger is communicated with the storage tank assembly, and the first heat exchanger is used for exchanging heat between raw materials and diesel oil; and the reaction heating furnace is communicated with the raw material outlet of the first heat exchanger, and the raw material subjected to heat exchange by the first heat exchanger enters the reaction heating furnace for heat exchange again. Through the technical scheme that this application provided, can solve the problem that the transformation cost is high among the prior art.

Description

Wax oil hydrocracking unit

Technical Field

The invention relates to the technical field of device modification, in particular to a wax oil hydrocracking device.

Background

Generally, a wax oil hydrocracking device comprises a reaction heating furnace and a reactor, and raw materials heated by the reaction heating furnace enter the reactor to be subjected to reaction cracking. In the process of reforming the light oil type of the wax oil hydrocracking device, the temperature of the raw materials entering the reactor is reduced from the original 195 ℃ to 148 ℃ after the raw materials are heated by the reaction heating furnace, and the feeding temperature cannot meet the reaction conditions of the reactor.

In the prior art, because the design power of the reaction heating furnace is low, the reaction heating furnace needs to be modified in order to increase the feeding temperature, the number of furnace tubes of the reaction heating furnace is increased, the load of the reaction heating furnace is increased, and the feeding temperature meets the reaction conditions of the reactor.

However, in the prior art, the investment for modifying the scheme of the reaction heating furnace is high due to the high cost of the furnace tube of the reaction heating furnace. Therefore, the prior art has the problem of high modification cost.

Disclosure of Invention

The invention provides a wax oil hydrocracking device, which aims to solve the problem of high modification cost in the prior art.

The invention provides a wax oil hydrocracking device, which comprises: the material storage tank assembly is used for storing raw materials; a diesel side line tower for producing diesel; the diesel oil tower bottom reboiling furnace is communicated with the diesel oil side tower and is used for exchanging heat with the diesel oil; the diesel oil heat exchange pipeline is provided with a diesel oil inlet and a diesel oil outlet, the diesel oil inlet is communicated with an outlet of the diesel oil side line tower, and the diesel oil outlet is communicated with an inlet of the reboiling furnace at the bottom of the diesel oil tower; the first heat exchanger is arranged on a diesel oil heat exchange pipeline, a raw material inlet of the first heat exchanger is communicated with the storage tank assembly, and the first heat exchanger is used for exchanging heat between raw materials and diesel oil; and the reaction heating furnace is communicated with the raw material outlet of the first heat exchanger, and the raw material subjected to heat exchange by the first heat exchanger enters the reaction heating furnace for heat exchange again.

Further, the wax oil hydrocracking device also comprises a second heat exchanger, the second heat exchanger is arranged on a pipeline between the first heat exchanger and the storage tank assembly, the second heat exchanger is provided with a second raw material channel and a second medium channel, the raw materials circulate in the second raw material channel, the heat exchange medium circulates in the second medium channel, and the second heat exchanger is used for pre-heat exchange of the raw materials.

Further, the wax oil hydrocracking unit also comprises: and the inlet of the reactor is communicated with the outlet of the reaction heating furnace, the outlet of the reactor is communicated with the raw material inlet of the second heat exchanger, and the reactor is used for cracking the raw material to obtain a primary processing product.

Further, the storage tank assembly includes: a cold raw material buffer tank; the hot raw materials buffer tank communicates with the cold raw materials buffer tank, and the hot raw materials buffer tank sets up in the low reaches of cold raw materials buffer tank, is provided with cold raw materials charge pump on the pipeline between hot raw materials buffer tank and the cold raw materials buffer tank, and the export and the second heat exchanger intercommunication of hot raw materials buffer tank are provided with hot raw materials charge pump on the pipeline between hot raw materials buffer tank and the second heat exchanger.

Furthermore, the wax oil hydrocracking device also comprises a diesel tower bottom reboiling pump, wherein the diesel tower bottom reboiling pump is arranged on a diesel heat exchange pipeline, or the diesel tower bottom reboiling pump is arranged on a pipeline between the diesel tower bottom reboiling furnace and a diesel side-line tower.

Further, the wax oil hydrocracking device also comprises an oil-gas-water separation component, the oil-gas-water separation component is communicated with the reactor, and the second heat exchanger is arranged on a pipeline between the oil-gas-water separation component and the reactor.

Further, the oil-gas-water separation assembly comprises: the thermal high-pressure separation tank is communicated with the second heat exchanger and is used for separating oil gas in the primary processing product; the hot low-pressure separation tank is communicated with the hot high-pressure separation tank, is positioned at the downstream of the hot high-pressure separation tank and is used for separating oil gas in the primary processing product; the cold high-pressure separation tank is communicated with the hot high-pressure separation tank, is positioned at the downstream of the hot high-pressure separation tank and is used for separating oil, water and gas in the primary processing product; the cold low-separating tank is communicated with the hot low-separating tank and the cold high-separating tank, the cold low-separating tank is positioned at the downstream of the hot low-separating tank and the cold high-separating tank, and the cold low-separating tank is used for separating oil, water and gas in the primary processing product.

Further, the wax oil hydrocracking device also comprises a first main stripping tower, the first main stripping tower is communicated with the oil-gas-water separation component, and the first main stripping tower is used for removing hydrogen sulfide in products.

Further, the wax oil hydrocracking unit also comprises: the flash tank is communicated with the first main stripping tower and is positioned at the downstream of the first main stripping tower and used for flashing light components in the primary processing product; and the fractionation heating furnace is communicated with the flash tank, is positioned at the downstream of the flash tank and is used for heating the product.

Further, the wax oil hydrocracking unit also comprises: and the second main stripping tower is provided with a first inlet and a second inlet, the first inlet is communicated with the outlet of the flash tank, the second inlet is communicated with the outlet of the fractionating heating furnace, the second main stripping tower is used for separating the primary processing product, and the outlet of the second main stripping tower is communicated with the inlet of the diesel side-draw tower.

By applying the technical scheme of the invention, the wax oil hydrocracking device comprises a storage tank assembly, a diesel oil side line tower, a diesel oil tower bottom reboiling furnace, a diesel oil heat exchange pipeline, a first heat exchanger and a reaction heating furnace. The diesel side tower is used for producing diesel, and the diesel tower bottom reboiling furnace is communicated with the diesel side tower to exchange heat with the diesel. Specifically, a diesel oil inlet of the diesel oil heat exchange pipeline is communicated with an outlet of the diesel oil side line tower, and a diesel oil outlet of the diesel oil heat exchange pipeline is communicated with an inlet of the diesel oil tower bottom reboiling furnace, so that diesel oil can circulate among the diesel oil heat exchange pipeline, the diesel oil side line tower and the diesel oil tower bottom reboiling furnace. Through set up first heat exchanger on diesel oil heat exchange pipeline, with the raw materials import and the storage tank subassembly intercommunication of first heat exchanger, can utilize the diesel oil of first heat exchanger of flowing through to carry out the heat transfer to the raw materials in order to promote the temperature of raw materials, then with the raw materials export intercommunication of reaction heating furnace and first heat exchanger, the raw materials after the heat transfer of first heat exchanger gets into the reaction heating furnace and carries out the heat transfer once more to make the feeding temperature of raw materials satisfy the reaction condition of reactor. By adopting the structure, the reaction heating furnace does not need to be reformed, and only the first heat exchanger is arranged on the diesel oil heat exchange pipeline, so that the feeding temperature of the raw materials can meet the reaction condition of the reactor, and the reforming cost can be remarkably reduced.

Drawings

The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:

fig. 1 shows a schematic diagram of a wax oil hydrocracking apparatus provided according to an embodiment of the present invention.

Wherein the figures include the following reference numerals:

10. a storage tank assembly; 11. a cold raw material buffer tank; 12. a hot raw material buffer tank; 13. a cold feed pump; 14. a hot feedstock feed pump;

20. a diesel side tower; 30. a reboiling furnace at the bottom of the diesel tower; 40. a diesel heat exchange pipeline; 50. a first heat exchanger; 60. a reaction heating furnace; 70. a second heat exchanger; 80. a reactor; 90. a reboiling pump at the bottom of the diesel tower;

100. an oil-gas-water separation assembly; 101. a hot high-pressure separation tank; 102. hot low-pressure separation tank; 103. cooling the high-pressure separation tank; 104. cooling and separating the tanks;

110. a first main stripper column; 120. a flash tank; 130. a fractionating heating furnace; 140. a second main stripper;

150. a tail oil circulating pipeline; 160. a tail oil pump; 170. a circulating diesel pipeline; 180. and (4) discharging the diesel from the device pump.

Detailed Description

The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. The following description of at least one exemplary embodiment is merely illustrative in nature and is in no way intended to limit the invention, its application, or uses. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

As shown in fig. 1, the embodiment of the present invention provides a wax oil hydrocracking apparatus, which includes a storage tank assembly 10, a diesel side tower 20, a diesel tower bottom reboiling furnace 30, a diesel heat exchange pipeline 40, a first heat exchanger 50, and a reaction heating furnace 60. Wherein, the storage tank assembly 10 is used for storing raw materials, and the diesel side tower 20 is used for producing diesel. The diesel tower bottom reboiling furnace 30 is communicated with the diesel side tower 20, so that the diesel tower bottom reboiling furnace 30 can be used for exchanging heat with diesel to improve the temperature of the diesel. Specifically, the diesel heat exchange pipeline 40 has a diesel inlet and a diesel outlet, the diesel inlet is communicated with the outlet of the diesel side tower 20, and the diesel outlet is communicated with the inlet of the reboiling furnace 30 at the bottom of the diesel tower. By adopting the structure, the diesel oil produced by the diesel oil side line tower 20 can enter the diesel oil heat exchange pipeline 40 through the outlet of the diesel oil side line tower 20, the diesel oil which completes circulation in the diesel oil heat exchange pipeline 40 can enter the diesel oil tower bottom reboiling furnace 30 through the diesel oil outlet, so that the diesel oil is reheated by the diesel oil tower bottom reboiling furnace 30, and the diesel oil reheated by the diesel oil tower bottom reboiling furnace 30 can enter the diesel oil side line tower 20 again. In this embodiment, the first heat exchanger 50 is disposed on the diesel heat exchange pipeline 40, a raw material inlet of the first heat exchanger 50 is communicated with the storage tank assembly 10, and the first heat exchanger 50 is used for exchanging heat between the raw material and the diesel. Specifically, the first heat exchanger 50 has a first raw material channel and a first medium channel, the raw material circulates in the first raw material channel, the diesel oil circulates in the first medium channel, and after the raw material enters the first heat exchanger from the raw material inlet of the first raw material channel, the raw material exchanges heat with the diesel oil in the first medium channel, so that the temperature of the raw material can be increased. By communicating the reaction heating furnace 60 with the raw material outlet of the first heat exchanger 50, the raw material heat-exchanged by the first heat exchanger 50 enters the reaction heating furnace 60 to exchange heat again, so that the feeding temperature meets the reaction conditions of the reactor.

Use the wax oil hydrocracking unit that this embodiment provided, through set up first heat exchanger 50 on diesel oil heat transfer pipeline 40, with the raw materials import and the storage tank subassembly 10 intercommunication of first heat exchanger 50, can utilize the diesel oil of first heat exchanger 50 of flowing through to carry out the heat transfer to the raw materials in order to promote the temperature of raw materials, then with the raw materials export intercommunication of reaction heating furnace 60 and first heat exchanger 50, the raw materials after the heat transfer of first heat exchanger 50 gets into reaction heating furnace 60 and carries out the heat transfer once more, thereby make the feed temperature of raw materials satisfy the reaction condition of reactor 80. By adopting the structure, the reaction heating furnace 60 does not need to be modified, and only the first heat exchanger 50 is arranged on the diesel heat exchange pipeline 40, so that the feeding temperature of the raw materials can meet the reaction condition of the reactor 80, and the modification cost can be obviously reduced. Moreover, by adopting the structure, the waste heat can be fully utilized, and the energy consumption of the device can be reduced.

In this embodiment, the wax oil hydrocracking apparatus further includes a second heat exchanger 70, and the second heat exchanger 70 is disposed on the pipeline between the first heat exchanger 50 and the storage tank assembly 10. Wherein, second heat exchanger 70 has second raw materials passageway and second medium passageway, and the raw materials circulates in second raw materials passageway, and heat transfer medium circulates in second medium passageway, and when the raw materials circulated in second raw materials passageway, heat transfer medium can heat the raw materials, can utilize second heat exchanger 70 to carry out the heat transfer in advance to the raw materials. Specifically, the outlet of the second material passage is communicated with the inlet of the first material passage, and the material pre-exchanged with heat by the second heat exchanger 70 enters the first heat exchanger 50, so that heat exchange can be performed again by the first heat exchanger 50, and the temperature of the material can be further increased. Specifically, the first heat exchanger 50 consists of one low pressure heat exchanger and the second heat exchanger 70 consists of three high pressure heat exchangers.

Wherein, the wax oil hydrocracking device also comprises a reactor 80, the inlet of the reactor 80 is communicated with the outlet of the reaction heating furnace 60, the raw material which is subjected to heat exchange again by the reaction heating furnace 60 enters the reactor 80, and the raw material can be cracked by the reactor 80 to obtain a primary processing product. Specifically, the outlet of the reactor 80 is communicated with the raw material inlet of the second heat exchanger 70, and the high-temperature medium flowing out of the reactor 80 can be used for heat exchange of the raw material.

Specifically, the design power of reaction heating furnace 60 is 132000KW, and if reaction heating furnace 60 is modified, the load of reaction heating furnace 60 is increased so that the feeding temperature satisfies the reaction condition of reactor 80, and the load needs to be increased to 180000KW. Since the furnace tube of the reaction heating furnace 60 is made of TP347L, the furnace tube is expensive, 2000 million investment is needed if the modification is completed, and the modification cost is very high. In this embodiment, by arranging the first heat exchanger 50 on the diesel heat exchange pipeline 40, the investment for modification is 200 million, and the capital is saved by 1800 ten million yuan by the scheme, so that the problem of high modification cost in the prior art can be solved.

In this embodiment, the accumulator tank assembly 10 includes a cold feed buffer tank 11 and a hot feed buffer tank 12. Wherein, hot raw materials buffer tank 12 and cold raw materials buffer tank 11 intercommunication, hot raw materials buffer tank 12 sets up the low reaches at cold raw materials buffer tank 11. Specifically, a cold raw material feeding pump 13 is arranged on a pipeline between the hot raw material buffer tank 12 and the cold raw material buffer tank 11, and the cold raw material feeding pump 13 can be used for pumping the raw material in the cold raw material buffer tank 11 into the hot raw material buffer tank 12. And the outlet of the hot raw material buffer tank 12 is communicated with the second heat exchanger 70, and a hot raw material feed pump 14 is arranged on a pipeline between the hot raw material buffer tank 12 and the second heat exchanger 70, so that the raw material in the hot raw material buffer tank 12 can be pumped into the second raw material channel of the second heat exchanger 70 by using the hot raw material feed pump 14, and the raw material is subjected to pre-heat exchange by using the second heat exchanger 70.

Wherein, still be provided with a plurality of heat exchangers between cold raw materials buffer tank 11 and hot raw materials buffer tank 12, can utilize a plurality of heat exchangers between cold raw materials buffer tank 11 and the hot raw materials buffer tank 12 to carry out preliminary heat transfer to the raw materials in the storage tank subassembly 10.

Specifically, the wax oil hydrocracking device further comprises a diesel tower bottom reboiling pump 90, wherein the diesel tower bottom reboiling pump 90 is arranged on the diesel heat exchange pipeline 40, or the diesel tower bottom reboiling pump 90 is arranged on a pipeline between the diesel tower bottom reboiling furnace 30 and the diesel side tower 20. In this embodiment, the diesel tower bottom reboiling pump 90 is disposed on the diesel heat exchange pipeline 40, and the diesel produced by the diesel side tower 20 can be pumped into the first heat exchanger 50 through the diesel heat exchange pipeline 40 by the diesel tower bottom reboiling pump 90, so as to exchange heat with the diesel in the first heat exchanger 50. In other embodiments, the diesel bottom reboiling pump 90 may be disposed on a pipeline between the diesel bottom reboiling furnace 30 and the diesel side tower 20, so that the diesel oil after heat exchange by the diesel bottom reboiling furnace 30 is pumped into the diesel side tower 20 by the diesel bottom reboiling pump 90.

In this embodiment, the wax oil hydrocracking apparatus further includes an oil-gas-water separation assembly 100, the oil-gas-water separation assembly 100 is communicated with the reactor 80, and the second heat exchanger 70 is disposed on a pipeline between the oil-gas-water separation assembly 100 and the reactor 80. Specifically, the oil-gas-water separation assembly 100 is located at the downstream of the reactor 80, a primary product obtained by cracking the reactor 80 enters the oil-gas-water separation assembly 100, and the oil-gas-water separation assembly 100 is used for separating oil, gas and water in the primary product.

Specifically, the oil-gas-water separation assembly 100 comprises a hot high-pressure separation tank 101, a hot low-pressure separation tank 102, a cold high-pressure separation tank 103 and a cold low-pressure separation tank 104. Wherein, the hot high-pressure separator tank 101 is communicated with the second heat exchanger 70, and the hot high-pressure separator tank 101 is used for separating oil gas in the primary processing product. The hot low-pressure separation tank 102 is communicated with the hot high-pressure separation tank 101, the hot low-pressure separation tank 102 is located at the downstream of the hot high-pressure separation tank 101, and the hot low-pressure separation tank 102 is used for separating oil gas in the primary processing products. The cold high-pressure separation tank 103 is communicated with the hot high-pressure separation tank 101, the cold high-pressure separation tank 103 is positioned at the downstream of the hot high-pressure separation tank 101, and the cold high-pressure separation tank 103 is used for separating oil, water and gas in the primary processing product. The cold low separating tank 104 is communicated with the hot low separating tank 102 and the cold high separating tank 103, the cold low separating tank 104 is positioned at the downstream of the hot low separating tank 102 and the cold high separating tank 103, and the cold low separating tank 104 is used for separating oil, water and gas in the primary processing product.

The wax oil hydrocracking device further comprises a first main stripping tower 110, the first main stripping tower 110 is communicated with the oil-gas-water separation assembly 100, and the first main stripping tower 110 is used for removing hydrogen sulfide in products. Specifically, the first main stripper 110 is in communication with the cold low drum 104 and the hot low drum 102, respectively.

In this embodiment, the wax oil hydrocracking apparatus further includes a flash drum 120 and a fractionation heating furnace 130. Wherein the flash tank 120 is communicated with the first main stripping column 110, the flash tank 120 is located at the downstream of the first main stripping column 110, and the flash tank 120 is used for flash evaporation of light components in the primary processing product. A fractionation heater 130 is in communication with the flash tank 120, the fractionation heater 130 being located downstream of the flash tank 120, the fractionation heater 130 being for heating the product. Moreover, a fractionation feed pump is disposed on a pipeline between the flash tank 120 and the fractionation heating furnace 130, and the flashed raw product may be pumped into the fractionation heating furnace 130 from the flash tank 120 by using the fractionation feed pump.

Specifically, the wax oil hydrocracking unit further includes a second main stripper 140. The second main stripping column 140 has a first inlet and a second inlet, the first inlet is communicated with the outlet of the flash drum 120, the second inlet is communicated with the outlet of the fractionating heating furnace 130, the second main stripping column 140 is used for separating the crude product, and the outlet of the second main stripping column 140 is communicated with the inlet of the diesel side column 20.

In the present embodiment, the second main stripper 140 has a first outlet and a second outlet. The first outlet of the second main stripping tower 140 is communicated with the inlet of the diesel side column 20, so that the separated and processed primary product can flow to the diesel side column 20 through the first outlet of the second main stripping tower 140, and diesel oil can be produced through the diesel side column 20.

In this embodiment, the wax oil hydrocracking apparatus further includes a circulating tail oil pipeline 150, the second outlet of the second main stripper 140 is communicated with the inlet of the circulating tail oil pipeline 150, the outlet of the circulating tail oil pipeline 150 is communicated with the hot feedstock buffer tank 12, and the tail oil remaining after separation in the second main stripper 140 can enter the hot feedstock buffer tank 12 through the circulating tail oil pipeline 150, so as to facilitate next processing. By transferring the tail oil of the second main stripper 140 into the hot raw material buffer tank 12, the utilization rate of the raw material can be improved, and the discharge of waste materials can be reduced. The tail oil pump 160 is provided in the circulating tail oil line 150, and the tail oil pump 160 of the second main stripper 140 may be used to pump the tail oil pump 160 into the hot material buffer tank 12.

In this embodiment, the wax oil hydrocracking apparatus further includes a circulating diesel oil pipeline 170, an inlet of the circulating diesel oil pipeline 170 is communicated with an outlet of the diesel oil side column 20, an outlet of the circulating diesel oil pipeline 170 is communicated with the cold raw material buffer tank 11, and a part of diesel oil produced by the diesel oil side column 20 and diesel oil containing impurities can enter the cold raw material buffer tank 11 through the circulating diesel oil pipeline 170 so as to facilitate next processing. By conveying part of diesel oil produced by the diesel oil side tower 20 and diesel oil containing impurities to the cold raw material buffer tank 11, the utilization rate of raw materials can be improved, and the emission of waste materials is reduced. And, a diesel oil outlet device pump 180 is provided on the circulating diesel oil pipeline 170, and a part of diesel oil produced by the diesel oil side tower 20 and diesel oil containing impurities can be pumped into the cold raw material buffer tank 11 by using the diesel oil outlet device pump 180.

Through the device that this embodiment provided, hot raw materials buffer tank 12 is gone into by cold raw materials charge pump 13 pump to the raw materials in the cold raw materials buffer tank 11, and at this in-process, cold raw materials can carry out preliminary heat transfer through a plurality of heat exchangers between cold raw materials buffer tank 11 and the hot raw materials buffer tank 12, and the raw materials after preliminary heat transfer exchange heat in second heat exchanger 70 with the high temperature medium that reactor 80 came out earlier to obtain the raw materials after the heat transfer in advance. Hot diesel oil is pumped into the first heat exchanger 50 through a diesel oil tower bottom reboiling pump 90, the raw material after pre-heat exchange exchanges heat with the hot diesel oil in the first heat exchanger 50 so as to increase the temperature of the raw material, and finally the raw material enters the reaction heating furnace 60 for heat exchange again and then undergoes reaction cracking in the reactor 80.

It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the present application. As used herein, the singular forms "a", "an", and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.

The relative arrangement of the components and steps, the numerical expressions and numerical values set forth in these embodiments do not limit the scope of the present invention unless specifically stated otherwise. Meanwhile, it should be understood that the sizes of the respective portions shown in the drawings are not drawn in an actual proportional relationship for the convenience of description. Techniques, methods, and apparatus known to those of ordinary skill in the relevant art may not be discussed in detail but are intended to be part of the specification where appropriate. In all examples shown and discussed herein, any particular value should be construed as exemplary only and not as limiting. Thus, other examples of the exemplary embodiments may have different values. It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, further discussion thereof is not required in subsequent figures.

In the description of the present invention, it is to be understood that the orientation or positional relationship indicated by the orientation words such as "front, rear, upper, lower, left, right", "lateral, vertical, horizontal" and "top, bottom", etc. are usually based on the orientation or positional relationship shown in the drawings, and are only for convenience of description and simplicity of description, and in the case of not making a reverse description, these orientation words do not indicate and imply that the device or element being referred to must have a specific orientation or be constructed and operated in a specific orientation, and therefore, should not be considered as limiting the scope of the present invention; the terms "inner and outer" refer to the inner and outer relative to the profile of the respective component itself.

For ease of description, spatially relative terms such as "over 8230 \ 8230;,"' over 8230;, \8230; upper surface "," above ", etc. may be used herein to describe the spatial relationship of one device or feature to another device or feature as shown in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. For example, if a device in the figures is turned over, devices described as "above" or "on" other devices or configurations would then be oriented "below" or "under" the other devices or configurations. Thus, the exemplary terms "at 8230; \8230; above" may include both orientations "at 8230; \8230; above" and "at 8230; \8230; below". The device may be otherwise variously oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein interpreted accordingly.

It should be noted that the terms "first", "second", and the like are used to define the components, and are only used for convenience of distinguishing the corresponding components, and the terms have no special meanings unless otherwise stated, and therefore, the scope of the present invention should not be construed as being limited.

The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A wax oil hydrocracking apparatus, characterized by comprising:

a holding tank assembly (10) for storing the feedstock;

a diesel side-line tower (20) for producing diesel;

the diesel tower bottom reboiling furnace (30) is communicated with the diesel side tower (20), and the diesel tower bottom reboiling furnace (30) is used for exchanging heat with diesel;

the diesel heat exchange pipeline (40) is provided with a diesel inlet and a diesel outlet, the diesel inlet is communicated with the outlet of the diesel side line tower (20), and the diesel outlet is communicated with the inlet of the diesel tower bottom reboiling furnace (30);

the first heat exchanger (50) is arranged on the diesel oil heat exchange pipeline (40), a raw material inlet of the first heat exchanger (50) is communicated with the storage tank assembly (10), and the first heat exchanger (50) is used for exchanging heat between raw materials and diesel oil;

the reaction heating furnace (60) is communicated with the raw material outlet of the first heat exchanger (50), and the raw material after heat exchange by the first heat exchanger (50) enters the reaction heating furnace (60) for heat exchange again;

the second heat exchanger (70), the second heat exchanger (70) is arranged on a pipeline between the first heat exchanger (50) and the storage tank assembly (10), the second heat exchanger (70) is provided with a second raw material channel and a second medium channel, the raw material circulates in the second raw material channel, a heat exchange medium circulates in the second medium channel, and the second heat exchanger (70) is used for pre-exchanging heat for the raw material;

the inlet of the reactor (80) is communicated with the outlet of the reaction heating furnace (60), the outlet of the reactor (80) is communicated with the raw material inlet of the second heat exchanger (70), and the reactor (80) is used for cracking the raw materials to obtain a primary processing product.

2. A wax oil hydrocracking unit according to claim 1, wherein said storage tank assembly (10) comprises:

a cold raw material buffer tank (11);

hot raw material buffer tank (12), with cold raw material buffer tank (11) intercommunication, hot raw material buffer tank (12) set up the low reaches of cold raw material buffer tank (11), hot raw material buffer tank (12) with be provided with cold raw material charge pump (13) on the pipeline between cold raw material buffer tank (11), the export of hot raw material buffer tank (12) with second heat exchanger (70) intercommunication, hot raw material buffer tank (12) with be provided with hot raw material charge pump (14) on the pipeline between second heat exchanger (70).

3. The wax oil hydrocracking apparatus according to claim 1, further comprising a diesel bottom reboiling pump (90), wherein the diesel bottom reboiling pump (90) is provided on the diesel heat exchange line (40), or the diesel bottom reboiling pump (90) is provided on a line between the diesel bottom reboiling furnace (30) and the diesel side column (20).

4. The wax oil hydrocracking apparatus according to claim 1, further comprising an oil-gas-water separation assembly (100), wherein the oil-gas-water separation assembly (100) is in communication with the reactor (80), and the second heat exchanger (70) is disposed on a pipeline between the oil-gas-water separation assembly (100) and the reactor (80).

5. A wax oil hydrocracking arrangement according to claim 4, wherein the oil-gas-water separation assembly (100) comprises:

the thermal high-pressure separation tank (101) is communicated with the second heat exchanger (70), and the thermal high-pressure separation tank (101) is used for separating oil gas in the primary processing product;

a hot low split tank (102) communicated with the hot high split tank (101), wherein the hot low split tank (102) is positioned at the downstream of the hot high split tank (101), and the hot low split tank (102) is used for separating oil and gas in the primary processing products;

the cold high-pressure separation tank (103) is communicated with the hot high-pressure separation tank (101), the cold high-pressure separation tank (103) is positioned at the downstream of the hot high-pressure separation tank (101), and the cold high-pressure separation tank (103) is used for separating oil, water and gas in a primary processing product;

the cold low-pressure separation tank (104) is communicated with the hot low-pressure separation tank (102) and the cold high-pressure separation tank (103), the cold low-pressure separation tank (104) is located at the downstream of the hot low-pressure separation tank (102) and the cold high-pressure separation tank (103), and the cold low-pressure separation tank (104) is used for separating oil, water and gas in a primary processing product.

6. A wax oil hydrocracking unit according to claim 4, further comprising a first main stripper (110), said first main stripper (110) being in communication with said oil-gas-water separation assembly (100), said first main stripper (110) being adapted to strip out hydrogen sulphide from the product.

7. A wax oil hydrocracking unit according to claim 6, further comprising:

a flash tank (120) in communication with the first main stripper (110), the flash tank (120) being located downstream of the first main stripper (110), the flash tank (120) being configured to flash light components of the as-processed product;

a fractionation furnace (130) in communication with the flash tank (120), the fractionation furnace (130) being located downstream of the flash tank (120), the fractionation furnace (130) being configured to heat the product.

8. The wax oil hydrocracking apparatus according to claim 7, further comprising:

a second main stripper (140) having a first inlet and a second inlet, the first inlet communicating with the outlet of the flash tank (120), the second inlet communicating with the outlet of the fractionation heating furnace (130), the second main stripper (140) separating the preform product, the outlet of the second main stripper (140) communicating with the inlet of the diesel side column (20).