CN113831935A

CN113831935A - Hydrocracking device

Info

Publication number: CN113831935A
Application number: CN202010581669.XA
Authority: CN
Inventors: 施俊林; 周能冬; 严钧; 丁健飞; 袁子中; 解协勤; 管家伟
Original assignee: China Petroleum and Chemical Corp
Current assignee: China Petroleum and Chemical Corp
Priority date: 2020-06-23
Filing date: 2020-06-23
Publication date: 2021-12-24
Anticipated expiration: 2040-06-23
Also published as: CN113831935B

Abstract

The invention relates to the technical field of petrochemical industry, and discloses a hydrocracking device, which comprises a reaction unit, a separation unit arranged at the downstream of the reaction unit, a desulfurization unit arranged at the downstream of the separation unit, and a first heat exchanger, wherein the first heat exchanger is provided with a first heat source inlet and a first heat source outlet for respectively supplying a heat source to and from, and a first cold source inlet and a first cold source outlet for respectively supplying a first cold source to and from, and the reaction unit is arranged to enable raw oil and hydrogen to generate a hydrocracking reaction so as to obtain a hydrocracking product; the separation unit is arranged to receive the hydrocracking product and make the hydrocracking product undergo gas-liquid separation; the desulfurization unit is arranged to receive the product oil discharged by the separation unit and perform desulfurization treatment on the product oil; the first heat source inlet is communicated with the reaction unit, the first heat source outlet is communicated with the separation unit, and the first cold source inlet is communicated with the desulfurization unit so as to be capable of receiving the desulfurization product oil. The hydrocracking unit enables the energy consumption of the hydrocracking process to be low.

Description

Hydrocracking device

Technical Field

The invention relates to the technical field of petrochemical industry, in particular to a hydrocracking device.

Background

Hydrocracking is an effective way for heavy oil conversion and is also an important means for producing clean fuels. Hydrocracking is one of petroleum refining processes, and is a process of converting heavy oil into gas, gasoline, jet fuel, diesel oil and the like through a cracking reaction under the conditions of heating, high hydrogen pressure and the presence of a catalyst.

The hydrocracking apparatus generally includes a reaction section, a separation section, an absorption stabilization section, a desulfurization section, and the like. The reaction part has high pressure and high temperature, and the heat exchange process of the reaction system is relatively fixed in the conventional design for reducing the safety risk and simultaneously reducing the investment. In the whole device, the heat source is reaction effluent, hot high-pressure gas and the cold source is raw oil, hydrogen, cold low-pressure oil and bottom oil of a stripping tower. A stripping tower is usually arranged in the desulfurization part to remove hydrogen sulfide in the hydrocracking products, and the desulfurized hydrocracking products enter a fractionating tower to be separated according to the distillation range. The temperature of the desulfurized hydrocracking product discharged from the stripping tower entering the fractionating tower is low, so that the energy consumption of the whole hydrocracking process is increased.

Disclosure of Invention

The invention aims to solve the problem of high energy consumption of a hydrocracking process in the prior art, and provides a hydrocracking device which enables the energy consumption of the hydrocracking process to be low.

In order to achieve the above object, an aspect of the present invention provides a hydrocracking apparatus, comprising:

the reaction unit is arranged to enable raw oil and hydrogen to generate hydrocracking reaction so as to obtain a hydrocracking product;

a separation unit disposed downstream of the reaction unit and configured to receive the hydrocracked product discharged from the reaction unit and subject the hydrocracked product to gas-liquid separation to obtain a gas and a product oil;

a desulfurization unit disposed downstream of the separation unit and configured to receive the product oil discharged by the separation unit and perform desulfurization treatment on the product oil to obtain a desulfurized product oil; and

the first heat exchanger is provided with a first heat source inlet and a first heat source outlet which are used for the inlet and the outlet of a heat source respectively, and a first cold source inlet and a first cold source outlet which are used for the inlet and the outlet of a first cold source respectively, wherein: the first heat source inlet is communicated with the reaction unit so as to be capable of receiving the hydrocracking product, the first heat source outlet is communicated with the separation unit, and the first cold source inlet is communicated with the desulfurization unit so as to be capable of receiving the desulfurization product oil.

According to the technical scheme, the first heat exchanger is arranged, so that the desulfurization product oil and the hydrocracking product discharged from the reaction unit can exchange heat, the desulfurization product oil has higher temperature before entering the fractionating tower, for example, the desulfurization product oil can be heated to 200-350 ℃ by the hydrocracking product, so that the fractionating effect is improved, the heat energy of the hydrocracking product is fully utilized, and the energy consumption of the whole system is reduced.

Preferably, the hydrocracking device comprises a second heat exchanger, the second heat exchanger is provided with a second heat source inlet and a second heat source outlet for respectively supplying heat sources to enter and exit, and a second cold source inlet and a second cold source outlet for respectively supplying reactants to enter and exit, wherein the reactants comprise the raw oil and the hydrogen, the second cold source inlet and the second cold source outlet are respectively provided with: the second heat source inlet is communicated with the first heat source outlet, the second heat source outlet is communicated with the separation unit so as to discharge the hydrocracking product subjected to heat exchange into the separation unit, and the second cold source outlet is communicated with the reaction unit so as to discharge the reactant to be reacted into the reaction unit.

Preferably, the reaction unit comprises a hydrofining reactor and a hydrocracking reactor arranged downstream of and in communication with the hydrofining reactor, wherein: the hydrofining reactor is provided with a hydrofining inlet and a hydrofining outlet, and the hydrocracking reactor is provided with a hydrocracking inlet and a hydrocracking outlet;

the hydrocracking unit comprises a third heat exchanger, the third heat exchanger is provided with a third heat source inlet and a third heat source outlet which are used for the inlet and the outlet of a heat source respectively, and a third cold source inlet and a third cold source outlet which are used for the inlet and the outlet of a cold source respectively, wherein: the third heat source inlet is communicated with the hydrofining outlet, the third heat source outlet is communicated with the hydrocracking inlet, the third cold source inlet is communicated with the second cold source outlet, and the third cold source outlet is communicated with the hydrofining inlet.

Preferably, the hydrocracking device comprises a heater, the heater is provided with a heating inlet and a heating outlet for respectively feeding and discharging materials to be heated, and the third cold source outlet is communicated with the hydrofining inlet through the heating inlet and the heating outlet.

Preferably, the hydrocracking unit includes a fourth heat exchanger, the fourth heat exchanger has a fourth heat source inlet and a fourth heat source outlet for respectively supplying heat source to enter and exit, and a fourth cold source inlet and a fourth cold source outlet for respectively supplying the raw oil to enter and exit, wherein: and the fourth cold source outlet is communicated with the second cold source inlet.

Preferably, the temperature of the heat source in the fourth heat exchanger is 80-200 ℃.

Preferably, the separation unit comprises a hot high-pressure separator having a first hot separation inlet for the substance to be separated, a first exhaust port for the separated gas to exit, and a first oil outlet for the separated product oil to exit, respectively, wherein: the first heat separation inlet is communicated with the second heat source outlet, and the first oil outlet is communicated with the desulfurization unit.

Preferably, the separation unit comprises a hot low-pressure separator arranged at the downstream of the hot high-pressure separator, the hot low-pressure separator is provided with a second hot separation inlet for the substance to be separated to enter and a second oil discharge port for the separated product oil to discharge, wherein the second hot separation inlet is communicated with the first oil discharge port, and the second oil discharge port is communicated with the desulfurization unit.

Preferably, the hydrocracking device comprises a fifth heat exchanger, the fifth heat exchanger is provided with a fifth heat source inlet and a fifth heat source outlet for heat source to enter and exit respectively, and a fifth cold source inlet and a fifth cold source outlet for hydrogen to enter and exit respectively, wherein: the fifth heat source inlet is communicated with the first exhaust port, and the fifth cold source outlet is communicated with the second cold source inlet.

Preferably, the separation unit comprises a separation mechanism, and the separation mechanism comprises a cold high-pressure separator, and the cold high-pressure separator is provided with a cold high-pressure separation inlet for the substance to be separated to enter and a cold high-pressure oil outlet for the separated product oil to discharge;

the hydrocracking device comprises a sixth heat exchanger, the sixth heat exchanger is arranged between the fifth heat exchanger and the cold high-pressure separator, and the sixth heat exchanger is arranged to cool the substances to be separated entering the cold high-pressure separator.

Preferably, the separation mechanism comprises a cold low-pressure separator arranged at the downstream of the cold high-pressure separator, the cold low-pressure separator is provided with a cold low-pressure separation inlet for the substance to be separated to enter and a cold low-pressure oil drain outlet for the separated product oil to drain, and the cold low-pressure separation inlet is communicated with the cold high-pressure oil drain outlet;

the sixth heat exchanger is provided with a sixth heat source inlet and a sixth heat source outlet for respectively supplying heat sources to enter and exit, and a sixth cold source inlet and a sixth cold source outlet for respectively supplying cold sources to enter and exit, wherein: the sixth heat source inlet is communicated with the fifth heat source outlet, the sixth heat source outlet is communicated with the cold high-pressure separation inlet of the cold high-pressure separator, the sixth cold source inlet is communicated with the cold low-pressure oil outlet of the cold low-pressure separator, and the sixth cold source outlet is communicated with the desulfurization unit.

Preferably, the separation unit comprises a seventh heat exchanger, the sixth heat exchanger is communicated with the cold high-pressure separator through the seventh heat exchanger, the seventh heat exchanger is provided with a seventh heat source inlet and a seventh heat source outlet for heat source to enter and exit respectively, wherein: and the seventh heat source inlet is communicated with the sixth heat source outlet, and the seventh heat source outlet is communicated with the inlet of the cold high-pressure separator.

Drawings

Fig. 1 is a schematic view of the overall structure of a hydrocracking apparatus according to a preferred embodiment of the present invention.

Description of the reference numerals

10-a hydrocracking unit; 11-a heater; 12-a reaction unit; 120-a hydrofining reactor; 122-a hydrocracking reactor; 14-a separation unit; 140-a hot high pressure separator; 142-a hot low pressure separator; 144 a-a cold high pressure separator; 144 b-a cold low pressure separator; 16-a desulfurization unit; 160-stripper column; 18 a-a first heat exchanger; 18 b-a second heat exchanger; 18 c-a third heat exchanger; 18 d-a fourth heat exchanger; 18 e-a fifth heat exchanger; 18 f-a sixth heat exchanger; 18 g-seventh heat exchanger.

Detailed Description

In the present invention, the use of directional terms such as "upper, lower, left and right" in the absence of a contrary explanation generally means that the directions shown in the drawings and the practical application are considered to be the same, and "inner and outer" mean the inner and outer of the outline of the component.

The invention provides a hydrocracking device, wherein the hydrocracking device 10 comprises a reaction unit 12, a separation unit 14, a desulfurization unit 16 and a first heat exchanger 18 a. The reaction unit 12 is configured to enable a hydrocracking reaction to occur between the feedstock oil and the hydrogen to obtain a hydrocracking product, where it is to be noted that the reaction unit 12 is filled with a corresponding catalyst to promote the hydrocracking reaction, and in addition, the hydrocracking reaction needs to be performed at a predetermined pressure and a predetermined temperature; the separation unit 14 is disposed downstream of the reaction unit 12, and the separation unit 14 is configured to receive the hydrocracking product discharged from the reaction unit 12 and subject the hydrocracking product to gas-liquid separation to obtain a gas and a product oil, it being understood that the separation unit 14 is capable of appropriately cooling the hydrocracking product to obtain a corresponding gas and a product oil; the desulfurization unit 16 is disposed downstream of the separation unit 14, and the desulfurization unit 16 is configured to receive the product oil discharged from the separation unit 14 and perform desulfurization treatment on the product oil, for example, hydrogen sulfide in the product oil can be removed, for example, desulfurization treatment can be performed on the product oil in a fractionation manner to remove hydrogen sulfide in the product oil, so as to obtain desulfurized product oil, and finally, the product oil enters a fractionation tower to obtain products separated according to a distillation range, that is, corresponding light oil products; first heat exchanger 18a has first heat source import and first heat source export and the first cold source import and the first cold source export that supplies first cold source business turn over respectively of supplying the heat source business turn over respectively, and it can be understood that compares and plays the cold source, and the heat source has higher temperature, and the heat source can carry out the heat transfer so that the cold source has higher temperature with the cold source like this, and wherein, heat source and cold source all can select according to the demand, wherein: the first heat source inlet is communicated with the reaction unit 12 to be able to receive the hydrocracking product, the first heat source outlet is communicated with the separation unit 14, and the first heat source inlet is communicated with the desulfurization unit 16 to be able to receive the desulfurization product oil, that is, the desulfurization product oil may be heated first before fractionation thereof, so that the desulfurization product oil may have a higher temperature before fractionation thereof. By arranging the first heat exchanger 18a, the desulfurization product oil can exchange heat with the hydrocracking product discharged from the reaction unit 12, so that the desulfurization product oil has a higher temperature before entering the fractionating tower, for example, the desulfurization product oil can be heated to 200-350 ℃ by the hydrocracking product, thereby not only improving the fractionation effect, but also fully utilizing the heat energy of the hydrocracking product and reducing the energy consumption of the whole system. Therein, the desulfurization unit 16 may include a stripper 160.

Wherein, the reaction unit 12 may include a hydrofining reactor 120 and a hydrocracking reactor 122 disposed downstream of the hydrofining reactor 120 and communicated with the hydrofining reactor 120, wherein: the hydrofinishing reactor 120 has a hydrofinishing inlet and a hydrofinishing outlet, and the hydrocracking reactor 122 has a hydrocracking inlet and a hydrocracking outlet. Thus, after the reactants containing the feedstock oil and hydrogen are added to the hydrofining reactor 120 for corresponding reactions such as impurity removal and saturation, the obtained product is added to the hydrocracking reactor 122 for corresponding reactions such as cracking reaction to obtain the hydrocracking product.

As shown in fig. 1, the hydrocracking apparatus 10 may include a second heat exchanger 18b, the second heat exchanger 18b having a second heat source inlet and a second heat source outlet for respectively supplying a heat source and a second cold source inlet and a second cold source outlet for respectively supplying a reactant to be reacted containing the feedstock oil and hydrogen to and from, wherein: the second heat source inlet is communicated with the first heat source outlet, the second heat source outlet is communicated with the separation unit 14 to discharge the heat-exchanged hydrocracking product into the separation unit 14, the second cold source outlet is communicated with the reaction unit 12 to discharge the reactant to be reacted into the reaction unit 12, the hydrocracking product passes through the first heat exchanger 18a and then enters the second heat exchanger 18b as a heat source to heat the cold source entering the second heat exchanger 18b, namely the reactant to be reacted containing the raw oil and the hydrogen, so that the heat energy of the hydrocracking product can be further utilized to heat the reactant to be reacted containing the raw oil and the hydrogen to a proper temperature. In addition, it should be noted that, since the hydrocracking product transfers part of the heat after passing through the first heat exchanger 18a, the hydrocracking product heats the reactant containing the raw oil and hydrogen to a suitable temperature after entering the second heat exchanger 18b, but does not heat to a higher temperature.

In order to fully utilize the heat energy, the hydrocracking apparatus 10 may include a third heat exchanger 18c, the third heat exchanger 18c having a third heat source inlet and a third heat source outlet for respectively supplying a heat source and a third cold source inlet and a third cold source outlet for respectively supplying a cold source and a cold source, wherein: the third heat source inlet is communicated with the hydrofining outlet, the third heat source outlet is communicated with the hydrocracking inlet, the third cold source inlet is communicated with the second cold source outlet, and the third cold source outlet is communicated with the hydrofining inlet. In this way, the heat energy of the product discharged from the hydrorefining reactor 120 can be utilized by the reactants containing the feedstock oil and hydrogen gas, but the reactants are heated to a suitable temperature, thereby further reducing energy consumption.

Cold hydrogen can be additionally introduced to the outlet of the hydrofining reactor 120 to cool down, so that the heat energy of the product discharged from the hydrofining reactor 120 is usually absorbed by the cold hydrogen, and the third heat exchanger 18c is provided, so that on one hand, the heat can be recovered, on the other hand, the cold hydrogen does not need to be additionally introduced to cool down, therefore, the hydrogen loss is reduced, the load of the recycle hydrogen compressor is also reduced, and the energy consumption of the whole hydrocracking device 10 is greatly reduced.

In order to heat the reactant to be heated to a suitable temperature, a heater 11 may be provided, the heater 11 having a heating inlet and a heating outlet for respectively feeding and discharging the material to be heated, and the third cold source outlet being in communication with the hydrofinishing inlet through the heating inlet and the heating outlet. In this way, the reactant containing the feedstock oil and hydrogen heated by the third heat exchanger 18c enters the heater 11 to be heated again, and then enters the hydrofining reactor 120 to perform a corresponding reaction. It should be noted that the maximum load of the heater 11 is usually designed according to the start-up, and during normal operation, the load of the heater 11 is lower, so that the heater 11 needs to heat the reactant containing the feedstock oil and hydrogen to a suitable temperature, for example, the reactant can be heated to 320-, VOC for short) is qualified.

It should be noted that the desulfurization product oil discharged from the desulfurization unit 16 is first heat-exchanged with the first heat exchanger 18a and then heated to a higher temperature, and the reactant is heated to a suitable temperature after passing through the second heat exchanger 18b, the third heat exchanger 18c and the heater 11, which have lower heat source temperatures, so that the heater 11 is maintained at the set heat load value.

In addition, a fourth heat exchanger 18d may be provided, the fourth heat exchanger 18d having a fourth heat source inlet and a fourth heat source outlet for respectively supplying heat sources to and from, and a fourth cold source inlet and a fourth cold source outlet for respectively supplying the raw oil to and from, wherein: the fourth cold source outlet is communicated with the second cold source inlet, so that raw oil can be preheated.

The heat source in the fourth heat exchanger 18d may comprise a low temperature heat source provided by the material discharged from the top of the fractionation tower or a low temperature heat source provided by the product distillate oil in order to utilize the lower heat energy in the system, i.e. to utilize the low temperature heat released in the hydrocracking system, and further, the temperature of the heat source in the fourth heat exchanger 18d is 80-200 ℃. Thus, the preheating of the raw oil is realized, and simultaneously, lower heat energy is fully utilized and is not wasted.

As shown in fig. 1, the separation unit 14 may include a hot high pressure separator 140, the hot high pressure separator 140 having a first hot separation inlet for the inlet of the substance to be separated, a first exhaust port for the exhaust of the separated gas, and a first oil discharge port for the exhaust of the separated product oil, respectively, wherein: the first heat separation inlet is communicated with the second heat source outlet, and the first oil discharge port is communicated with a desulfurization unit 16. The hydrocracking product discharged from the second heat exchanger 18b is fed as a material to be separated into the hot high-pressure separator 140 to be cooled to achieve gas-liquid separation. The separated product oil may be discharged to a desulfurization unit 16 for desulfurization treatment.

In addition, a hot low-pressure separator 142 may be disposed downstream of the hot high-pressure separator 140, and the hot low-pressure separator 142 has a second hot separation inlet into which the to-be-separated material enters and a second oil discharge outlet through which the separated product oil is discharged, respectively, wherein the second hot separation inlet is communicated with the first oil discharge outlet, and the second oil discharge outlet is communicated with the desulfurization unit 16. It will be appreciated that the product oil separated by the hot high pressure separator 140 may be introduced into the hot low pressure separator 142 for further gas-liquid separation, and the resulting product oil may be discharged into the desulfurization unit 16 for desulfurization treatment, thereby improving the separation effect and the yield of the separated material.

In addition, a fifth heat exchanger 18e may be provided, the fifth heat exchanger 18e having a fifth heat source inlet and a fifth heat source outlet for the heat source to enter and exit respectively, and a fifth cold source inlet and a fifth cold source outlet for the hydrogen gas to enter and exit respectively, wherein: the fifth heat source inlet is communicated with the first exhaust port, and the fifth cold source outlet is communicated with the second cold source inlet, so that the gas separated by the hot high-pressure separator 140 can be used as a heat source of the fifth heat exchanger 18e to heat the hydrogen serving as the raw material for the hydrocracking reaction, so as to heat the hydrogen to a proper temperature.

The separation unit 14 may include a separation mechanism, which may include a cold high pressure separator 144a, the cold high pressure separator 144a having a cold high pressure separation inlet for the entry of the material to be separated and a cold high pressure oil drain for the discharge of the separated product oil, respectively; meanwhile, a sixth heat exchanger 18f may be provided, the sixth heat exchanger 18f may be disposed between the fifth heat exchanger 18e and the cold high-pressure separator 144a, and the sixth heat exchanger 18f may be disposed to cool the matter to be separated entering the cold high-pressure separator 144 a.

Preferably, the separation mechanism may include a cold low-pressure separator 144b disposed downstream of the cold high-pressure separator 144a, the cold low-pressure separator 144b having a cold low-pressure separation inlet into which the matters to be separated enter and a cold low-pressure oil drain outlet through which the separated product oil is discharged, respectively, the cold low-pressure separation inlet communicating with the cold high-pressure oil drain outlet, the product discharged from the cold high-pressure separator 144a being discharged into the cold low-pressure separator 144 b; the sixth heat exchanger 18f has a sixth heat source inlet and a sixth heat source outlet for the heat source to enter and exit respectively, and a sixth cold source inlet and a sixth cold source outlet for the cold source to enter and exit respectively, wherein: the sixth heat source inlet is communicated with the fifth heat source outlet, the sixth heat source outlet is communicated with the cold high-pressure separation inlet of the cold high-pressure separator 144a, the sixth cold source inlet is communicated with the cold low-pressure oil outlet of the cold low-pressure separator 144b, and the sixth cold source outlet is communicated with the desulfurization unit 16. In this way, the gas separated by the hot high pressure separator 140 may pass through the fifth heat exchanger 18e and enter the sixth heat exchanger 18f to serve as a heat source for the sixth heat exchanger 18f to heat the product oil discharged from the cold low pressure oil discharge port of the cold low pressure separator 144b, and then the product oil enters the desulfurization unit 16 for desulfurization.

In order to further improve the cold low-pressure separation effect, a seventh heat exchanger 18g may be provided, the sixth heat exchanger 18f may be communicated with the cold high-pressure separator 144a through the seventh heat exchanger 18g, the seventh heat exchanger 18g has a seventh heat source inlet and a seventh heat source outlet for the heat source to enter and exit, respectively, wherein: the seventh heat source inlet is communicated with the sixth heat source outlet, the seventh heat source outlet is communicated with the cold high-pressure separation inlet of the cold high-pressure separator 144a, wherein the gas discharged from the sixth heat exchanger 18f can enter the seventh heat exchanger 18g for cooling, for example, air cooling, and then the gas enters the cold high-pressure separator 144a for gas-liquid separation, and the separated product oil can enter the cold low-pressure separator 144b located at the downstream for gas-liquid separation again.

The operation will be described below by taking the hydrocracking apparatus 10 shown in fig. 1 as an example. The raw oil is preheated to 50-190 ℃ by the fourth heat exchanger 18d, meanwhile, the hydrogen is heated to 100-; raw oil and hydrogen enter the hydrofining reactor 120 to perform corresponding reaction to obtain an intermediate reaction product; the intermediate reaction product is cooled to 340-400 ℃ by the third heat exchanger 18c and then enters the hydrocracking reactor 122 for corresponding reaction to obtain a hydrocracking product; the hydrocracking product as a heat source sequentially passes through the first heat exchanger 18a and the second heat exchanger 18b, then enters the hot high-pressure separator 140 for gas-liquid separation, the separated product oil is discharged into the hot low-pressure separator 142 for gas-liquid separation, the separated product oil is discharged into the stripping tower 160 for desulfurization treatment, the separated gas as a heat source sequentially passes through the fifth heat exchanger 18e, the sixth heat exchanger 18f and the seventh heat exchanger 18g, then enters the cold low-pressure separator 144 for gas-liquid separation, the separated product oil is discharged into the sixth heat exchanger 18f for heating, and then is discharged into the stripping tower 160 for desulfurization treatment.

Taking the hydrocracking system using the hydrocracking device 10 shown in fig. 1 as an example, the total load of the heater 11 and the fractionation feed heating furnace can be reduced by at least 15%, the power of the recycle hydrogen compressor can be reduced by 8%, and the energy-saving effect is obvious.

The preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, numerous simple modifications can be made to the technical solution of the invention, including combinations of the individual specific technical features in any suitable way. The invention is not described in detail in order to avoid unnecessary repetition. Such simple modifications and combinations should be considered within the scope of the present disclosure as well.

Claims

1. A hydrocracking apparatus characterized in that the hydrocracking apparatus (10) comprises:

the reaction unit (12), the reaction unit (12) is configured to enable the raw oil and the hydrogen to generate hydrocracking reaction so as to obtain a hydrocracking product;

a separation unit (14), said separation unit (14) being arranged downstream of said reaction unit (12), and said separation unit (14) being arranged to be able to receive said hydrocracked product discharged by said reaction unit (12) and to subject said hydrocracked product to a gas-liquid separation to obtain a gas and a product oil;

a desulfurization unit (16), wherein the desulfurization unit (16) is arranged at the downstream of the separation unit (14), and the desulfurization unit (16) is arranged to receive the product oil discharged by the separation unit (14) and perform desulfurization treatment on the product oil to obtain desulfurized product oil; and

a first heat exchanger (18a), the first heat exchanger (18a) having a first heat source inlet and a first heat source outlet for respectively supplying a heat source and a first cold source inlet and a first cold source outlet for respectively supplying a first cold source, wherein: the first heat source inlet is communicated with the reaction unit (12) so as to be capable of receiving the hydrocracking product, the first heat source outlet is communicated with the separation unit (14), and the first cold source inlet is communicated with the desulfurization unit (16) so as to be capable of receiving the desulfurization product oil.

2. The hydrocracking apparatus according to claim 1, wherein the hydrocracking apparatus (10) comprises a second heat exchanger (18b), the second heat exchanger (18b) having a second heat source inlet and a second heat source outlet for respectively supplying heat sources in and out, and a second heat sink inlet and a second heat sink outlet for respectively supplying reactants to be reacted containing the feedstock oil and hydrogen in and out, wherein: the second heat source inlet is communicated with the first heat source outlet, the second heat source outlet is communicated with the separation unit (14) so as to discharge the hydrocracking products subjected to heat exchange into the separation unit (14), and the second cold source outlet is communicated with the reaction unit (12) so as to discharge the reactant to be reacted into the reaction unit (12).

3. The hydrocracking apparatus according to claim 2, wherein the reaction unit (12) comprises a hydrofinishing reactor (120) and a hydrocracking reactor (122) disposed downstream of the hydrofinishing reactor (120) and in communication with the hydrofinishing reactor (120), wherein: the hydrofinishing reactor (120) having a hydrofinishing inlet and a hydrofinishing outlet, the hydrocracking reactor (122) having a hydrocracking inlet and a hydrocracking outlet;

the hydrocracking device (10) comprises a third heat exchanger (18c), the third heat exchanger (18c) is provided with a third heat source inlet and a third heat source outlet for respectively supplying heat sources to and from and a third cold source inlet and a third cold source outlet for respectively supplying cold sources to and from, wherein: the third heat source inlet is communicated with the hydrofining outlet, the third heat source outlet is communicated with the hydrocracking inlet, the third cold source inlet is communicated with the second cold source outlet, and the third cold source outlet is communicated with the hydrofining inlet.

4. The hydrocracking apparatus according to claim 3, wherein the hydrocracking apparatus (10) comprises a heater (11), the heater (11) having a heating inlet and a heating outlet for the material to be heated to enter and exit, respectively, and the third cold source outlet communicating with the hydrofinishing inlet through the heating inlet and the heating outlet.

5. The hydrocracking apparatus according to claim 2, wherein the hydrocracking apparatus (10) comprises a fourth heat exchanger (18d), the fourth heat exchanger (18d) having a fourth heat source inlet and a fourth heat source outlet for the entry and exit of a heat source, respectively, and a fourth cold source inlet and a fourth cold source outlet for the entry and exit of the feedstock, respectively, wherein: and the fourth cold source outlet is communicated with the second cold source inlet.

6. Hydrocracking plant according to claim 5, characterized in that the temperature of the heat source in the fourth heat exchanger (18d) is between 80 and 200 ℃.

7. The hydrocracking apparatus according to any one of claims 2 to 6, wherein the separation unit (14) comprises a hot high pressure separator (140), the hot high pressure separator (140) having a first hot separation inlet for the entry of the material to be separated, a first exhaust for the exit of the separated gas and a first oil outlet for the exit of the separated product oil, respectively, wherein: the first heat separation inlet is communicated with the second heat source outlet, and the first oil outlet is communicated with the desulfurization unit (16).

8. The hydrocracking apparatus according to claim 7, wherein the separation unit (14) comprises a hot low pressure separator (142) disposed downstream of the hot high pressure separator (140), the hot low pressure separator (142) having a second hot separation inlet for the entry of the material to be separated and a second oil drain for the discharge of the separated product oil, wherein the second hot separation inlet is in communication with the first oil drain and the second oil drain is in communication with the desulfurization unit (16).

9. The hydrocracking apparatus of claim 7, wherein the hydrocracking apparatus (10) comprises a fifth heat exchanger (18e), the fifth heat exchanger (18e) having a fifth heat source inlet and a fifth heat source outlet for the ingress and egress of heat sources, respectively, and a fifth cold source inlet and a fifth cold source outlet for the ingress and egress of hydrogen, respectively, wherein: the fifth heat source inlet is communicated with the first exhaust port, and the fifth cold source outlet is communicated with the second cold source inlet.

10. The hydrocracking apparatus of claim 9, wherein the separation unit (14) comprises a separation mechanism comprising a cold high pressure separator (144a), the cold high pressure separator (144a) having a cold high pressure separation inlet for entry of a material to be separated and a cold high pressure oil drain for discharge of separated product oil, respectively;

the hydrocracking device (10) comprises a sixth heat exchanger (18f), the sixth heat exchanger (18f) is arranged between the fifth heat exchanger (18e) and the cold high-pressure separator (144a), and the sixth heat exchanger (18f) is arranged to cool the substance to be separated entering the cold high-pressure separator (144 a).

11. The hydrocracking apparatus according to claim 10, wherein the separation mechanism comprises a cold low pressure separator (144b) disposed downstream of the cold high pressure separator (144a), the cold low pressure separator (144b) having a cold low pressure separation inlet for entry of the material to be separated and a cold low pressure oil drain for discharge of the separated product oil, respectively, the cold low pressure separation inlet communicating with the cold high pressure oil drain;

the sixth heat exchanger (18f) is provided with a sixth heat source inlet and a sixth heat source outlet for the heat source to enter and exit respectively, and a sixth cold source inlet and a sixth cold source outlet for the cold source to enter and exit respectively, wherein: the sixth heat source inlet is communicated with the fifth heat source outlet, the sixth heat source outlet is communicated with the cold high-pressure separation inlet of the cold high-pressure separator (144a), the sixth cold source inlet is communicated with the cold low-pressure oil discharge port of the cold low-pressure separator (144b), and the sixth cold source outlet is communicated with the desulfurization unit (16).

12. The hydrocracking apparatus of claim 11, wherein the separation unit (14) comprises a seventh heat exchanger (18g), the sixth heat exchanger (18f) being in communication with the cold high pressure separator (144a) through the seventh heat exchanger (18g), the seventh heat exchanger (18g) having a seventh heat source inlet and a seventh heat source outlet for the supply of heat to and from, respectively, wherein: the seventh heat source inlet is communicated with the sixth heat source outlet, and the seventh heat source outlet is communicated with the inlet of the cold high-pressure separator (144 a).