CN112457151B

CN112457151B - System and method for refining coal hydrogasification oil product

Info

Publication number: CN112457151B
Application number: CN202011333888.2A
Authority: CN
Inventors: 王浩强; 马志超; 王蕾; 吴小军; 马丽荣
Original assignee: ENN Science and Technology Development Co Ltd
Current assignee: ENN Science and Technology Development Co Ltd
Priority date: 2020-11-24
Filing date: 2020-11-24
Publication date: 2023-02-21
Anticipated expiration: 2040-11-24
Also published as: CN112457151A

Abstract

The present disclosure relates to a refining system and a method for coal hydrogasification oil products, wherein the refining system comprises a de-heavy tower, a primary distillation tower, a naphthalene tower and a benzene tower; the heavy pyrene removing tower is provided with a crude pyrene oil inlet and is used for removing heavy pyrene oil so as to obtain light pyrene oil on the top of the heavy pyrene removing tower; the primary distillation tower is provided with a light pyrene oil inlet and a crude benzene oil inlet, and is used for rectifying the light pyrene oil and the crude benzene oil to obtain a light component oil product at the tower top of the primary distillation tower and obtain a heavy component oil product at the tower bottom of the primary distillation tower; the naphthalene tower is provided with a light component oil product inlet and is used for rectifying the light component oil product to obtain benzene-rich fraction at the tower top of the naphthalene tower and obtain refined naphthalene at the tower bottom of the naphthalene tower; the benzene tower is provided with a benzene-rich fraction inlet and a crude benzene inlet, and is used for rectifying the benzene-rich fraction and the crude benzene to obtain refined benzene at the tower top of the benzene tower, so that the additional value of the oil product is improved.

Description

System and method for refining coal hydrogasification oil product

Technical Field

The disclosure relates to the technical field of oil product manufacturing and production, in particular to a system and a method for refining coal hydrogasification oil products.

Background

The coal hydro-gasification technology is an important way for clean and efficient utilization of coal.

The coal hydrogenation gasification produces methane, semicoke and oil, because the oil is the mixture of multiple components, the coal hydrogenation gasification technology is different according to the oil boiling point at present, through the mode of condensation with the oil condensation step by step to crude pyrene oil, crude benzene oil and crude benzene.

However, the three oil products, namely the crude pyrene oil, the crude benzene oil and the crude benzene, are all mixtures of multiple components, and if the three oil products are directly sold as finished oil, the added value of the oil products is low, and the competitiveness of the hydro-gasification technology is reduced.

Disclosure of Invention

In order to solve the technical problems or at least partially solve the technical problems, the present disclosure provides a system and a method for refining coal hydrogasification oil products.

In a first aspect, the present disclosure provides a system for refining coal hydrogasification oil products, comprising a de-heavy tower, a preliminary distillation tower, a naphthalene tower and a benzene tower;

the heavy pyrene removing tower is provided with a crude pyrene oil inlet for crude pyrene oil to enter the heavy pyrene removing tower, and the heavy pyrene removing tower is used for removing heavy pyrene oil so as to obtain light pyrene oil on the top of the heavy pyrene removing tower;

the primary distillation tower is provided with a light pyrene oil inlet and a crude benzene oil inlet for crude benzene oil to enter the primary distillation tower, the light pyrene oil inlet is communicated with the top of the de-heavy tower so that the light pyrene oil can enter the primary distillation tower, the primary distillation tower is used for rectifying the light pyrene oil and the crude benzene oil so as to obtain light component oil products at the top of the primary distillation tower and obtain heavy component oil products at the bottom of the primary distillation tower;

the naphthalene tower is provided with a light component oil product inlet communicated with the tower top of the primary distillation tower, the light component oil product inlet is used for allowing the light component oil product to enter the naphthalene tower, the naphthalene tower is used for rectifying the light component oil product so as to obtain benzene-rich fraction at the tower top of the naphthalene tower, and refined naphthalene is obtained at the tower bottom of the naphthalene tower;

the benzene tower is provided with a benzene-rich fraction inlet and a crude benzene inlet for crude benzene to enter the benzene tower, the benzene-rich fraction inlet is communicated with the tower top of the naphthalene tower so that the benzene-rich fraction enters the benzene tower, and the benzene tower is used for rectifying the benzene-rich fraction and the crude benzene so as to obtain refined benzene at the tower top of the benzene tower.

The refining system for the coal hydrogasification oil product comprises a heavy component removal tower, a primary distillation tower, a naphthalene tower and a benzene tower, wherein crude pyrene oil is firstly introduced into the heavy component removal tower, heavy component removal treatment is carried out on the crude pyrene oil through the heavy component removal tower to obtain light pyrene oil, then the light pyrene oil and the crude benzene oil are introduced into the primary distillation tower to be subjected to rectification treatment to obtain light component oil, then the light component oil is introduced into the naphthalene tower to be subjected to rectification treatment to obtain refined naphthalene and benzene-rich fraction, and then the benzene-rich fraction and the crude benzene are introduced into the benzene tower to be subjected to rectification treatment to obtain refined benzene. Meanwhile, the heavy component in the crude pyrene oil is prevented from being wasted by the repeated heating of a subsequent tower by performing the heavy component removing treatment on the crude pyrene oil, and the situation that the heavy component of the crude pyrene oil is excessively heated to cause viscosity increase and coking can be prevented. In addition, the crude pyrene oil, the crude benzene oil and the crude benzene are added into different towers in a grading manner for rectification, so that the components of the oil products are effectively matched, and the situation that the heat load is too high and too much ineffective heat is consumed due to the fact that three oil products are added into one tower for rectification at the same time is avoided.

Optionally, the refining system further comprises a fluorene tower and a fluorene melt crystallizer;

the fluorene tower is provided with a heavy component oil inlet communicated with the tower bottom of the primary distillation tower, the heavy component oil inlet is used for allowing the heavy component oil to enter the fluorene tower, the fluorene tower is used for rectifying the heavy component oil so as to obtain fluorene oil at the tower top of the fluorene tower, and the fluorene-removed oil is obtained at the tower bottom of the fluorene tower;

the fluorene melt crystallizer is provided with a fluorene oil pipeline which is communicated with the top of the fluorene tower and can be used for the fluorene oil to enter, and the fluorene melt crystallizer is used for carrying out melt crystallization treatment on the fluorene oil to obtain refined fluorene.

Optionally, the refining system further comprises a phenanthrene tower and a phenanthrene melt crystallizer;

the phenanthrene tower is provided with a fluorene removing oil inlet communicated with the bottom of the fluorene tower, the fluorene removing oil inlet is used for allowing fluorene removing oil to enter the phenanthrene tower, the phenanthrene tower is used for rectifying the fluorene removing oil so as to obtain phenanthrene oil on the top of the phenanthrene tower, and pyrene-rich oil is obtained at the bottom of the phenanthrene tower;

the phenanthrene melt crystallizer is provided with a phenanthrene oil pipeline which is communicated with the top of the phenanthrene tower and can be used for the phenanthrene oil to enter, and the phenanthrene melt crystallizer is used for carrying out melt crystallization treatment on the phenanthrene oil so as to obtain refined phenanthrene.

Optionally, the refining system further comprises a pyrene melt crystallizer;

the pyrene melting crystallizer is provided with a pyrene-rich oil pipeline communicated with the bottom of the phenanthrene tower and allowing the pyrene-rich oil to enter, and the pyrene melting crystallizer is used for carrying out melting crystallization treatment on the pyrene-rich oil to obtain refined pyrene.

Optionally, the fluorene melt crystallizer is provided with a fluorene crystallization residual oil discharge port, and the fluorene crystallization residual oil discharge port is communicated with the fluorene tower, so that fluorene crystallization residual oil formed after the fluorene oil is subjected to melt crystallization treatment enters the fluorene tower;

the pyrene melting crystallizer is provided with a pyrene crystallization residual oil discharge port, the phenanthrene melting crystallizer is provided with a pyrene crystallization residual oil discharge port, and the phenanthrene crystallization residual oil discharge port and the pyrene crystallization residual oil discharge port are communicated with the phenanthrene tower, so that phenanthrene crystallization residual oil formed after the phenanthrene oil is subjected to melting crystallization treatment and pyrene crystallization residual oil formed after the pyrene-rich oil is subjected to melting crystallization treatment enter the phenanthrene tower.

Optionally, a benzene tower reboiler is arranged at the bottom of the benzene tower, and the top of the fluorene tower is communicated with the benzene tower reboiler, so that the fluorene oil exchanges heat in the benzene tower reboiler to provide a heat source for the benzene tower reboiler;

the tower bottom of the naphthalene tower is provided with a naphthalene tower reboiler, and the tower top of the phenanthrene tower is communicated with the naphthalene tower reboiler, so that the phenanthrene oil exchanges heat in the naphthalene tower reboiler, and a heat source is provided for the naphthalene tower reboiler.

Optionally, the bottom of the benzene column has a toluene-rich component discharge port, and the toluene-rich component discharge port is communicated with the naphthalene column, so that at least part of the toluene-rich component formed at the bottom of the benzene column during rectification in the benzene column enters the naphthalene column for rectification.

Optionally, the refining system further comprises a desulfurization device;

the heavy tower backward flow jar of taking off of heavy tower the first distillation column backward flow jar of first distillation column the naphthalene tower backward flow jar of naphthalene tower the benzene tower backward flow jar of benzene tower the fluorene tower backward flow jar of fluorene tower and the phenanthrene tower backward flow jar of phenanthrene tower all has gas discharge port, each gas discharge port all with desulphurization unit intercommunication, desulphurization unit is used for to by each the gas of gas discharge port combustion carries out desulfurization treatment, desulphurization unit has the gas vent, the gas vent respectively with take off heavy tower heating furnace of heavy tower the first distillation column heating furnace of first distillation column the fluorene tower heating furnace of fluorene tower and the phenanthrene tower heating furnace intercommunication of phenanthrene tower.

In a second aspect, the present disclosure provides a method for refining an oil product by using the system for refining a coal hydrogasification oil product as described above, the method comprising:

introducing the crude pyrene oil into a de-heavy tower, and performing de-heavy treatment on the crude pyrene oil at a first preset pressure and a first preset temperature to obtain light pyrene oil at the tower top of the de-heavy tower;

introducing the light pyrene oil and the crude benzene oil into a primary distillation tower, and rectifying the light pyrene oil and the crude benzene oil at a second preset temperature to obtain a light component oil product at the tower top of the primary distillation tower and a heavy component oil product at the tower bottom of the primary distillation tower;

introducing the light component oil product into a naphthalene tower, and rectifying the light component oil product at a third preset temperature to obtain benzene-rich fraction at the tower top of the naphthalene tower and obtain refined naphthalene at the tower bottom of the naphthalene tower;

and introducing the benzene-rich fraction and the crude benzene into a benzene tower, and rectifying the benzene-rich fraction and the crude benzene at a fourth preset temperature to obtain refined benzene at the tower top of the benzene tower.

The method for refining the oil by using the refining system for the coal hydro-gasification oil comprises the steps of firstly introducing crude pyrene oil into a heavy removal tower, carrying out heavy removal treatment on the crude pyrene oil through the heavy removal tower to obtain light pyrene oil, then introducing the light pyrene oil and crude benzene oil into a primary distillation tower to carry out rectification treatment to obtain light component oil, then introducing the light component oil into a naphthalene tower to carry out rectification treatment to obtain refined naphthalene and benzene-rich fraction, and then introducing the benzene-rich fraction and the crude benzene into a benzene tower to carry out rectification treatment to obtain refined benzene. Meanwhile, the heavy component in the crude pyrene oil is prevented from being wasted by the repeated heating of a subsequent tower by performing the heavy component removing treatment on the crude pyrene oil, and the situation that the heavy component of the crude pyrene oil is excessively heated to cause viscosity increase and coking can be prevented. In addition, the crude pyrene oil, the crude benzene oil and the crude benzene are added into different towers in a grading manner for rectification, so that the components of the oil products are effectively matched, and the situation that the heat load is too high and too much ineffective heat is consumed due to the fact that three oil products are added into one tower for rectification at the same time is avoided.

Optionally, after the step of introducing the light pyrene oil and the crude benzene oil into a primary distillation tower, and performing rectification treatment on the light pyrene oil and the crude benzene oil at a second preset temperature to obtain a light component oil at the tower top of the primary distillation tower, and obtain a heavy component oil at the tower bottom of the primary distillation tower, the method further includes:

introducing at least part of the heavy component oil product into a fluorene tower, and rectifying the heavy component oil product at a second preset pressure and a fifth preset temperature to obtain fluorene oil at the tower top of the fluorene tower and defluorinated oil at the tower bottom of the fluorene tower;

and carrying out melt crystallization treatment on the fluorene oil to obtain refined fluorene.

Optionally, after the step of introducing at least part of the heavy component oil into the fluorene tower, rectifying the heavy component oil at a fifth preset temperature to obtain fluorene oil at the tower top of the fluorene tower, and obtaining the defluorinated oil at the tower bottom of the fluorene tower, the method further includes:

introducing at least part of the defluorinated oil into a phenanthrene tower, and rectifying the defluorinated oil under a third preset pressure and a sixth preset temperature to obtain phenanthrene oil at the tower top of the phenanthrene tower and pyrene-rich oil at the tower bottom of the phenanthrene tower;

and carrying out melt crystallization treatment on the phenanthrene oil and the pyrene-rich oil to obtain refined phenanthrene and refined pyrene.

Optionally, the method further includes:

introducing fluorene crystallization residual oil obtained by carrying out melt crystallization treatment on the fluorene oil into the fluorene tower;

and introducing phenanthrene crystallized residual oil and pyrene crystallized residual oil obtained after carrying out melting crystallization treatment on the phenanthrene oil and the pyrene-rich oil into the phenanthrene tower.

Optionally, the method further includes:

introducing at least part of the fluorene oil into a benzene tower reboiler to enable the fluorene oil to exchange heat in the benzene tower reboiler and provide a heat source for the benzene tower reboiler;

and introducing at least part of the phenanthrene oil into a naphthalene tower reboiler to ensure that the phenanthrene oil exchanges heat in the naphthalene tower reboiler and provide a heat source for the naphthalene tower reboiler.

Optionally, after the step of introducing the benzene-rich fraction and the crude benzene into the benzene column and performing rectification treatment on the benzene-rich fraction and the crude benzene at a fourth preset temperature to obtain refined benzene at the top of the benzene column, the method further includes:

passing at least a portion of the toluene-rich component formed at the bottom of the benzene column into the naphthalene column to subject the at least a portion of the toluene-rich component to a rectification process in the naphthalene column.

Optionally, the method further includes:

carrying out desulfurization treatment on gas exhausted from a heavy component removal tower reflux tank, a primary distillation tower reflux tank, a naphthalene tower reflux tank, a benzene tower reflux tank, a fluorene tower reflux tank and a phenanthrene tower reflux tank by a desulfurization device;

and introducing the gas subjected to desulfurization treatment into a de-heavy tower heating furnace, a primary distillation tower heating furnace, a fluorene tower heating furnace and a phenanthrene tower heating furnace.

Drawings

The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the present disclosure and together with the description, serve to explain the principles of the disclosure.

In order to more clearly illustrate the embodiments or technical solutions in the prior art of the present disclosure, the drawings used in the embodiments or technical solutions in the prior art description will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to these drawings without inventive labor.

FIG. 1 is a block diagram of a system for refining coal hydrogasification oil according to an embodiment of the present disclosure;

FIG. 2 is a schematic structural diagram of a system for refining coal hydrogasification oil according to an embodiment of the present disclosure;

FIG. 3 is a schematic structural diagram of a desulfurization device in a system for refining coal hydrogasification oil according to an embodiment of the present disclosure;

fig. 4 is a schematic structural diagram of a fluorene melting crystallizer in a refining system of coal hydrogasification oil products according to an embodiment of the present disclosure;

FIG. 5 is a first schematic flow chart illustrating a method for refining an oil product by using a system for refining a coal hydrogasification oil product according to an embodiment of the present disclosure;

fig. 6 is a schematic flow diagram of a second method for refining an oil product by using a system for refining a coal hydrogasification oil product according to an embodiment of the present disclosure.

Wherein, 1, a heavy component removing tower; 11. a crude pyrene oil inlet; 12. a de-heaving column condenser; 13. a reflux tank of the de-weighting tower; 131. a first gas discharge port; 14. a heavy component removal tower heating furnace; 2. a preliminary distillation tower; 21. a light pyrene oil inlet; 22. a crude benzene oil inlet; 23. a primary distillation tower condenser; 24. a reflux tank of the primary distillation tower; 241. a second gas discharge port; 25. a heating furnace of a primary distillation tower; 26. a heavy component oil outlet; 3. a naphthalene column; 31. a light component oil inlet; 32. a naphthalene column condenser; 33. a naphthalene column reflux drum; 331. a third gas discharge port; 34. a naphthalene column reboiler; 4. a benzene column; 41. a benzene-rich fraction inlet; 42. a crude benzene inlet; 43. a benzene tower condenser, 44 and a benzene tower reflux tank; 441. a fourth gas discharge port; 45. a benzene-water separator; 46. a benzene column reboiler; 47. a toluene-rich component discharge port; 5. a fluorene tower; 51. a heavy component oil inlet; 52. a fluorene oil heat exchanger; 53. a fluorene tower reflux tank; 531. a fifth gas discharge port; 54. a fluorene oil buffer tank; 55. a fluorene tower heating furnace; 56. a defluorinated oil outlet; 57. a fluorene melt crystallizer; 571. a fluorene oil inlet; 572. a fluorene oil conduit; 573. a heat exchange medium inlet; 574. a heat exchange medium channel; 575. a heat exchange medium outlet; 576. a residual fluorene crystal oil discharge port; 6. a phenanthrene tower; 61. a defluorinated oil inlet; 62. a phenanthrene oil heat exchanger; 63. a phenanthrene tower reflux tank; 631. a sixth gas discharge port; 64. a phenanthrene oil buffer tank; 65. a phenanthrene tower heating furnace; 66. an pyrene-rich oil outlet; 67. a pyrene-rich oil buffer tank; 68. a phenanthrene melt crystallizer; 69. a pyrene melt crystallizer; 7. a desulfurization unit; 71. an air inlet; 72. and (7) an exhaust port.

Detailed Description

In order that the above objects, features and advantages of the present disclosure may be more clearly understood, aspects of the present disclosure will be further described below. It should be noted that the embodiments and features of the embodiments of the present disclosure may be combined with each other without conflict.

In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present disclosure, but the present disclosure may be practiced otherwise than as described herein; it is to be understood that the embodiments disclosed in the specification are only a few embodiments of the present disclosure, and not all embodiments.

Oil products produced by coal hydro-gasification are a mixture of multiple components, and in the existing coal hydro-gasification process, the oil products are gradually condensed into crude pyrene oil, crude benzene oil and crude benzene in a condensation mode according to different boiling points of the oil products.

As can be seen from the following tables 1 to 3, the crude pyrene oil, the crude benzene oil and the crude benzene are all mixtures of various components, and if the three oil products are directly sold as finished oil, the added value of the oil products is low, and the competitiveness of the hydro-gasification technology is reduced.

TABLE 1 composition of crude pyrene oil under typical conditions

Components

Benzene (III)

Naphthalene

Pyrene

Anthracene

Phenanthrene

Fluorene compound

Toluene

H ₂ S

wt％

0.47

1.33

51.08

0.26

12.17

3.93

0.17

Micro-scale

TABLE 2 composition of crude benzene oil under typical conditions

Components

Benzene (III)

Naphthalene

Pyrene

Anthracene

Phenanthrene

Fluorene compounds

Toluene

H ₂ S

wt％

70.37

18.34

1.08

0.08

1.86

1.67

3.95

Micro-scale

TABLE 3 composition of crude benzene for typical conditions

Components	Benzene (III)	Toluene	Water (W)
				wt％	93.33	2.47	4

Based on this, the embodiment provides a system and a method for refining coal hydrogasification oil product, which refine crude pyrene oil, crude benzene oil and crude benzene to obtain high-purity high-added-value components such as refined benzene, refined naphthalene, refined fluorene, refined phenanthrene and refined pyrene, and further improve the added value of the oil product.

The system and the method for refining the coal hydrogasification oil product are described in detail by the following specific examples:

referring to fig. 1 and 2, the present embodiment provides a system for refining coal hydrogasification oil, including: a heavy component removal tower 1, a primary distillation tower 2, a naphthalene tower 3 and a benzene tower 4.

Wherein, heavy tower 1 that takes off has and is used for supplying crude pyrene oil to get into the crude pyrene oil inlet 11 in heavy tower 1 that takes off, and heavy tower 1 that takes off is used for taking off heavy processing to crude pyrene oil to obtain light pyrene oil at the top of the tower that takes off heavy tower 1.

The primary tower 2 is provided with a light pyrene oil inlet 21 and a crude benzene oil inlet 22 for crude benzene oil to enter the primary tower 2, the light pyrene oil inlet 21 is communicated with the top of the de-heavy tower 1 so that the light pyrene oil can enter the primary tower 2, the primary tower 2 is used for rectifying the light pyrene oil and the crude benzene oil so as to obtain light component oil products on the top of the primary tower 2, and heavy component oil products are obtained on the bottom of the primary tower 2.

Wherein, the light pyrene oil inlet 21 and the crude benzene oil inlet 22 can be the same inlet, and during the specific operation, the light pyrene oil and the crude benzene oil are mixed and then are introduced into the primary distillation tower 2 from the inlets. Of course, the light pyrene oil inlet 21 and the crude benzene oil inlet 22 may be two different inlets, and the light pyrene oil and the crude benzene oil respectively enter the preliminary distillation tower 2 from the corresponding inlets.

The naphthalene tower 3 is provided with a light component oil product inlet 31 communicated with the top of the primary distillation tower 2, the light component oil product inlet 31 is used for allowing light component oil products to enter the naphthalene tower 3, the naphthalene tower 3 is used for rectifying the light component oil products so as to obtain benzene-rich fraction at the top of the naphthalene tower 3, and refined naphthalene is obtained at the bottom of the naphthalene tower 3.

The benzene tower 4 is provided with a benzene-rich fraction inlet 41 and a crude benzene inlet 42 for feeding crude benzene into the benzene tower 4, the benzene-rich fraction inlet 41 is communicated with the tower top of the naphthalene tower 3 for feeding the benzene-rich fraction into the benzene tower 4, and the benzene tower 4 is used for rectifying the benzene-rich fraction and the crude benzene to obtain refined benzene at the tower top of the benzene tower 4.

The benzene-rich fraction inlet 41 and the crude benzene inlet 42 may be the same inlet, and in the specific operation, the benzene-rich fraction and the crude benzene are mixed and then introduced into the benzene column 4 through the inlets. Of course, the benzene-rich fraction inlet 41 and the crude benzene inlet 42 may be two different inlets, and the benzene-rich fraction and the crude benzene enter the benzene column 4 through the respective inlets.

Specifically, the crude pyrene oil produced by hydro-gasification is introduced into a heavy component removing tower 1 from a crude pyrene oil inlet 11, heavy components which account for about 30% of the crude pyrene oil are removed under a first preset pressure and a first preset temperature, the heavy components are prevented from being repeatedly heated in subsequent towers, energy is saved, the situation that the heavy components are coked due to viscosity increase caused by overheating is prevented, and most impurities in the product are removed.

The first preset pressure is specifically the pressure at the top of the de-heavy column 1, and the first preset pressure can be set to be 8-12 KPa, that is, less than one atmosphere. The first preset temperature may specifically be: the temperature of the top of the tower is 270 to 280 ℃, and the temperature of the bottom of the tower is 360 to 370 ℃. The first preset temperature can be specifically set according to actual requirements.

That is to say, heavy component removing tower 1 adopts the mode of vacuum distillation to rectify continuously, guarantees that the component (light pyrene oil) of boiling point ≤ pyrene is all distilled from heavy component removing tower 1 overhead, and the top oil gas enters heavy component removing tower reflux tank 13 after the heavy component removing tower condenser 12 condensation and forms light pyrene oil, and partly reflux with the reflux ratio of 3. The heavy component is at the bottom of the de-heavy tower 1, part of the heavy component at the bottom of the de-heavy tower is reheated to be gaseous by a de-heavy tower heating furnace 14 and then returns to the de-heavy tower 1 to provide the required heat for the rectification treatment of the de-heavy tower 1, and the other part of the heavy component is taken as product asphalt to be extracted and transported outside, and then the heavy component can be taken as a raw material of modified asphalt or used for preparing fuel oil or chemicals through hydrocracking.

And (3) the components of the light pyrene oil are close to those of the crude benzene oil, the light pyrene oil and the crude benzene oil are introduced into a primary distillation tower 2, and the light pyrene oil and the crude benzene oil are subjected to rectification treatment at a second preset temperature. The light pyrene oil and the crude benzene oil are close in components and are introduced into the primary distillation tower 2 together, so that the crude benzene oil is prevented from entering the heavy component removal tower 1 in advance to cause increase of heat load. Specifically, the preliminary distillation tower 2 adopts the mode of atmospheric distillation for continuous distillation, wherein the atmospheric pressure is one atmosphere. Ensuring that all components (light component oil products) with the boiling point less than or equal to naphthalene are distilled from the top of the primary tower 2, and the heavy component oil products are separated from the tower bottom. The second preset temperature may specifically be: the temperature at the top of the tower is 230-235 ℃, and the temperature at the bottom of the tower is 360-365 ℃. The second preset temperature can be specifically set according to actual requirements. The oil gas at the tower top is condensed by a primary tower condenser 23 and then enters a primary tower reflux tank 24 to form light component oil, one part of the light component oil refluxes according to the reflux ratio of 3. A part of heavy component oil at the bottom of the primary tower 2 is reheated to be gaseous by the primary tower heating furnace 25 and then returns to the primary tower 2 to provide heat required by the rectification treatment of the primary tower 2, and the other part of heavy component oil enters the fluorene tower 5 from a heavy component oil outlet 26.

And the light component oil enters a naphthalene tower 3, and the light component oil is rectified at a third preset temperature. Specifically, the naphthalene tower 3 adopts a normal pressure rectification mode for continuous rectification, and the third preset temperature specifically may be: the temperature of the top of the tower is 130-135 ℃, and the temperature of the bottom of the tower is 215-220 ℃. The third preset temperature can be specifically set according to actual requirements. The oil gas at the tower top is condensed by a naphthalene tower condenser 32 and then enters a naphthalene tower reflux tank 33 to form benzene-rich fraction, one part of the benzene-rich fraction refluxes with the reflux ratio of 2. The benzene-rich fraction is specifically a mixture of benzene, toluene and water. One part of the components at the bottom of the naphthalene tower 3 is reheated by a naphthalene tower reboiler 34 to become gaseous and then returns to the naphthalene tower 3 to provide the required heat for the rectification treatment of the naphthalene tower 3, and the other part of the components is output as a product of refined naphthalene, wherein the purity of the refined naphthalene can reach more than 99 percent, and the yield is more than 83 percent.

And (3) enabling the benzene-rich fraction to be close to the crude benzene in composition, introducing the benzene-rich fraction and the crude benzene into a benzene tower 4, and rectifying the benzene-rich fraction and the crude benzene at a fourth preset temperature. Because the benzene-rich fraction is close to the crude benzene component, the benzene-rich fraction and the crude benzene component are introduced into the benzene tower 4 together, which is beneficial to avoiding the increase of heat load caused by the fact that the crude benzene enters the de-heavy tower 1, the primary distillation tower 2 and the naphthalene tower 3 in advance. Specifically, the benzene column 4 is continuously rectified by means of atmospheric rectification, where atmospheric pressure is one atmosphere. The fourth preset temperature may specifically be: the temperature at the top of the tower is 95-100 ℃, and the temperature at the bottom of the tower is 125-130 ℃. Oil gas at the top of the tower is condensed by a benzene tower condenser 43 and then enters a benzene tower reflux tank 44 to form a benzene-water mixture, one part of the mixture reflows at a reflux ratio of 3-4.

The bottom of the benzene column 4 has a toluene-rich component discharge port 47 for discharging the toluene-rich component formed at the bottom of the benzene column 4, and preferably, the toluene-rich component discharge port 47 is communicated with the naphthalene column 3, so that a part of the toluene-rich component is returned to the naphthalene column 3, and the rectification treatment is performed again in the naphthalene column 3 to improve the yield of naphthalene and benzene. The other part of the toluene-rich component is reheated to a gaseous state by the benzene column reboiler 46 and returned to the benzene column 4 to provide the heat required for the rectification treatment of the benzene column 4.

The crude pyrene oil, the crude benzene oil and the crude benzene are separated and refined to obtain high-purity refined benzene and refined naphthalene, so that the additional value of the oil product is improved.

The system for refining coal hydrogasification oil provided by this embodiment is provided with a heavy component removal tower 1, a primary distillation tower 2, a naphthalene tower 3 and a benzene tower 4, and firstly introduces crude pyrene oil into the heavy component removal tower 1, and performs heavy component removal treatment on the crude pyrene oil through the heavy component removal tower 1 to obtain light pyrene oil, and then introduces the light pyrene oil and the crude benzene oil into the primary distillation tower 2 to perform rectification treatment to obtain light component oil, and then introduces the light component oil into the naphthalene tower 3 to perform rectification treatment to obtain refined naphthalene and benzene-rich fraction, and then introduces the benzene-rich fraction and the crude benzene into the benzene tower 4 to perform rectification treatment to obtain refined benzene, that is, the refined naphthalene and the refined benzene with high additional value components are obtained through the above method, so that the defect of low additional value of the existing oil is overcome, not only the hydrogasification process is deepened, but also the additional value of the oil is greatly improved, and further the competitiveness of the whole coal hydrogasification technology is improved. Meanwhile, the heavy component in the crude pyrene oil is prevented from being wasted by the repeated heating of a subsequent tower by performing the heavy component removing treatment on the crude pyrene oil, and the situation that the heavy component of the crude pyrene oil is excessively heated to cause viscosity increase and coking can be prevented. In addition, the crude pyrene oil, the crude benzene oil and the crude benzene are added into different towers in a grading manner for rectification, so that the components of the oil products are effectively matched, and the situation that the heat load is too high and too much ineffective heat is consumed due to the fact that three oil products are added into one tower for rectification at the same time is avoided.

Further, the system for refining coal hydrogasification oil product of this embodiment further includes: a fluorene tower 5 and a fluorene melt crystallizer 57.

The fluorene tower 5 is provided with a heavy component oil inlet 51 communicated with the tower bottom of the primary distillation tower 2, the heavy component oil inlet 51 is used for feeding heavy component oil into the fluorene tower 5, the fluorene tower 5 is used for rectifying the heavy component oil to obtain fluorene oil on the tower top of the fluorene tower 5, and the fluorene-removed oil is obtained on the tower bottom of the fluorene tower 5. The bottom of the fluorene tower 5 is provided with a defluorinated oil outlet 56 for discharging defluorinated oil. The fluorene melting crystallizer 57 has a fluorene oil pipeline 572 communicated with the top of the fluorene tower 5 and allowing fluorene oil to enter, and the fluorene melting crystallizer 57 is used for performing melting crystallization treatment on the fluorene oil to obtain refined fluorene.

Specifically, the heavy component oil enters the fluorene tower 5 through the heavy component oil inlet 51, and the heavy component oil is rectified at a second preset pressure and a fifth preset temperature. The second preset pressure is specifically the top pressure of the fluorene tower 5, and the second preset pressure may be specifically set to 8 to 10kPa, that is, less than one atmosphere. That is, the fluorene tower 5 is continuously rectified by vacuum rectification. The fifth preset temperature may specifically be: the temperature of the top of the tower is 215-220 ℃, and the temperature of the bottom of the tower is 315-320 ℃. The fluorene oil obtained by rectification treatment is distilled out from the top of the fluorene tower 5. Preferably, the top of the fluorene tower 5 is communicated with the benzene tower reboiler 46, so that the fluorene oil distilled from the top of the fluorene tower 5 exchanges heat in the benzene tower reboiler 46, a heat source is provided for the benzene tower reboiler 46, heat is effectively matched, and energy consumption is reduced. Then, the fluorene oil enters a fluorene oil heat exchanger 52, and enters a fluorene tower reflux tank 53 after twice condensation. Specifically, the system further comprises a fluorene oil buffer tank 54, and the fluorene oil buffer tank 54 is specifically communicated with the fluorene oil reflux tank and is used for storing fluorene oil. One part of the fluorene oil in the fluorene oil reflux tank refluxes in a reflux ratio of 3.5.

The fluorene oil in the fluorene oil buffer tank 54 enters a melt crystallizer of fluorene. Referring to fig. 4, specifically, the fluorene melt crystallizer 57 has a fluorene oil inlet 571, a heat exchange medium inlet 573, a heat exchange medium channel 574 and a heat exchange medium outlet 575. The fluorene oil passage communicates with the fluorene oil inlet 571. Fluorene oil enters the fluorene oil channel from a fluorene oil inlet 571 and stands still, and a heat exchange medium enters the heat exchange medium pipeline from a heat exchange medium inlet 573. The heat exchange medium is preferably circulating heat conducting oil, intermittent operation is adopted, the flow rate of the heat exchange medium is constant at 3-4m/s, the initial temperature of an inlet of the heat exchange medium is 180 ℃, the temperature is gradually reduced to 90-95 ℃ at the speed of 5-6 ℃/h, at the moment, the component mainly containing fluorene is crystallized, after the non-crystallized residual liquid is discharged, the temperature of the heat exchange medium is gradually increased to 105-110 ℃ at the speed of 3-4 ℃/h for sweating operation, in the process, the crystallized components except for fluorene are gradually melted, sweat after remelting is discharged and mixed with the residual liquid discharged before, and the sweat is called fluorene crystallization residual oil. Specifically, the fluorene melt crystallizer 57 has a fluorene crystal residue oil discharge port 576, and the fluorene crystal residue oil discharge port 576 is communicated with the fluorene tower 5, so that the fluorene crystal residue oil is returned to the fluorene tower 5 through the fluorene crystal residue oil discharge port 576 for recycling. The residual crystal is refined fluorene with the content of 99 percent, the temperature of a cooling medium is increased to 130-140 ℃ at the speed of 6-8 ℃/h to completely melt the fluorene, and the fluorene is collected, and the yield of the fluorene is more than 80 percent.

Through setting up fluorene oil buffer tank 54, utilize fluorene oil buffer tank 54 to store fluorene oil, can effectual smooth control enter into the fluorene oil mass in fluorene melt crystallizer 57.

The system for refining the coal hydrogasification oil product of the embodiment further comprises a phenanthrene tower 6, a phenanthrene melt crystallizer 68 and a pyrene melt crystallizer 69. The phenanthrene tower 6 is provided with a fluorene removing oil inlet 61 communicated with the bottom of the fluorene tower 5, the fluorene removing oil inlet 61 is used for allowing fluorene removing oil to enter the phenanthrene tower 6, the phenanthrene tower 6 is used for rectifying the fluorene removing oil so as to obtain phenanthrene oil on the top of the phenanthrene tower 6, and pyrene-rich oil is obtained on the bottom of the phenanthrene tower 6.

The phenanthrene melt crystallizer 68 is provided with a phenanthrene pipeline which is communicated with the top of the phenanthrene tower 6 and is used for allowing phenanthrene oil to enter, and the phenanthrene melt crystallizer 68 is used for carrying out melt crystallization treatment on the phenanthrene oil so as to obtain refined phenanthrene. The pyrene melting crystallizer 69 is provided with a pyrene-rich oil pipeline communicated with the bottom of the phenanthrene tower 6 and allowing pyrene-rich oil to enter, and the pyrene melting crystallizer 69 is used for performing melting crystallization treatment on the pyrene-rich oil to obtain refined pyrene.

The specific structures and the use principles of the phenanthrene melt crystallizer 68 and the pyrene melt crystallizer 69 are the same as those of the fluorene melt crystallizer 57, and are not described herein again.

Specifically, the fluorene removing oil at the bottom of the fluorene tower 5 is discharged through a fluorene removing oil outlet 56, a part of the fluorene removing oil is reheated by a fluorene tower heating furnace 55 and then returns to the fluorene tower 5 to provide heat required for the rectification treatment of the fluorene tower 5, and the other part of the fluorene removing oil enters the phenanthrene tower 6 to be rectified at a third preset pressure and a sixth preset temperature. The third preset pressure is specifically the top pressure of the phenanthrene tower 6, and the third preset pressure can be set to be 8-10 kPa, namely, less than one atmosphere, that is, the phenanthrene tower 6 is continuously rectified in a reduced pressure rectification mode. The sixth preset temperature may specifically be: the temperature at the top of the tower is 245-250 ℃, and the temperature at the bottom of the tower is 335-340 ℃. The sixth preset temperature can be specifically set according to actual requirements.

Preferably, the top of the phenanthrene tower 6 is communicated with the naphthalene tower reboiler 34, so that phenanthrene oil distilled from the top of the phenanthrene tower 6 exchanges heat in the naphthalene tower reboiler 34, a heat source is provided for the naphthalene tower reboiler 34, heat is effectively matched, and energy consumption is reduced. The phenanthrene oil is formed after heat exchange, enters the phenanthrene oil heat exchanger 62, and enters the phenanthrene oil reflux tank after two-step condensation. Specifically, this system is still including rich and useless oil buffer tank 64, rich and useless oil buffer tank 64 specifically with rich and useless oil reflux tank intercommunication for store rich and useless oil. One part of the phenanthrene oil in the phenanthrene oil reflux tank refluxes according to a reflux ratio of 4.

The phenanthrene oil in the phenanthrene oil buffer tank 64 enters the phenanthrene melt crystallizer 68, the phenanthrene oil is added into the phenanthrene melt crystallizer 68 and stands, a heat exchange medium is introduced into a heat exchange medium pipeline, the heat exchange medium is preferably circulating heat conduction oil, intermittent operation is adopted, the flow rate of the heat exchange medium is constant and is 3-4m/s, the initial temperature of the heat exchange medium inlet is 160 ℃, the temperature is gradually reduced to 80-85 ℃ at the speed of 5-6 ℃/h, at the moment, phenanthrene-based components are crystallized out, after non-crystallized residual liquid is discharged, the temperature of a tube pass heat exchange medium is gradually increased to 90-95 ℃ at the speed of 3-4 ℃/h, sweating operation is carried out, in the process, crystallized components except phenanthrene are gradually melted, sweat after remelting is discharged and mixed with the residual liquid discharged before, and the melted components are called phenanthrene crystal residual oil. Specifically, the phenanthrene melt crystallizer 68 is provided with a phenanthrene crystal residual oil discharge port, and the phenanthrene crystal residual oil discharge port is communicated with the phenanthrene tower 6, so that the phenanthrene crystal residual oil is fed back into the phenanthrene tower 6 for recycling. The residual crystal is refined phenanthrene with the content of 99 percent, the cooling medium is heated to 120-130 ℃ at the speed of 6-8 ℃/h to completely melt the phenanthrene, and the phenanthrene is collected, so that the yield of the phenanthrene reaches over 80 percent.

The tower bottom of phenanthrene tower 6 has rich pyrene oil export 66, and this system still includes rich pyrene oil buffer tank 67, and rich pyrene oil buffer tank 67 communicates with rich pyrene oil export 66 for store rich pyrene oil. One part of the pyrene-rich oil at the bottom of the phenanthrene tower 6 enters the phenanthrene tower 6 after being reheated by the phenanthrene tower heating furnace 65, the other part of the pyrene-rich oil enters the pyrene-rich oil buffer tank 67, the content of pyrene in the pyrene-rich oil reaches more than 83%, and the pyrene-rich oil can directly enter the pyrene melting crystallizer 69 without being rectified to enrich pyrene fractions. Adding the pyrene-rich oil into a pyrene melting crystallizer 69 and standing, introducing a heat exchange medium, wherein the heat exchange medium is preferably circulating heat conduction oil, adopting intermittent operation, the flow rate of the heat exchange medium is constant at 3-4m/s, the initial temperature of the heat exchange medium inlet is 200 ℃, the temperature is gradually reduced to 130-135 ℃ at the speed of 4-5 ℃/h, at the moment, a component mainly containing pyrene is crystallized, after discharging uncrystallized residual liquid, gradually heating the tube-pass heat exchange medium to 140-145 ℃ at the speed of 3-4 ℃/h to perform sweating operation, gradually melting the crystallized components except pyrene in the process, discharging sweat after re-melting, and mixing the sweat with the residual liquid discharged before to obtain pyrene crystallization residual oil. Specifically, the pyrene melt crystallizer 69 is provided with a pyrene crystallization residual oil discharge port, and the pyrene crystallization residual oil discharge port is communicated with the phenanthrene tower 6, so that pyrene crystallization residual oil is fed back into the phenanthrene tower 6 for recycling. And (3) heating the cooling medium to 170-180 ℃ at the speed of 5-6 ℃/h to completely melt the pyrene, and collecting, wherein the yield of the pyrene is more than 80%.

The fluorene oil, the phenanthrene oil and the pyrene-rich oil enter a static melting crystallizer for refining, the operation steps are similar, the cooling and sweating procedures are carried out, the cooled and sweated crystallization residual oil is returned to the corresponding tower, namely, the fluorene crystallization residual oil is returned to the fluorene tower 5, and the phenanthrene crystallization residual oil and the pyrene crystallization residual oil are returned to the phenanthrene tower 6, so that the raw material loss is reduced, and the yield of fluorene, phenanthrene and pyrene is increased.

As shown in fig. 2 and 3, the system further includes a desulfurization unit 7. The desulfurizer 7 has an inlet 71 and an outlet 72. Wherein, the heavy component removal tower reflux tank 13, the preliminary distillation tower reflux tank 24, the naphthalene tower reflux tank 33, the benzene tower reflux tank 44, the fluorene tower reflux tank 53 and the phenanthrene tower reflux tank 63 are all provided with gas discharge ports. Wherein the de-heaving tower reflux tank 13 has a first gas discharge port 131, the preliminary distillation tower reflux tank 24 has a second gas discharge port 241, the naphthalene tower reflux tank 33 has a third gas discharge port 331, the benzene tower reflux tank 44 has a fourth gas discharge port 441, the fluorene tower reflux tank 53 has a fifth gas discharge port 531, and the phenanthrene tower reflux tank 63 has a sixth gas discharge port 631. Each gas discharge port is communicated with a gas inlet 71 of the desulfurization device 7, the desulfurization device 7 is used for performing desulfurization treatment on the gas discharged from each gas discharge port, and the gas after desulfurization treatment is discharged through a gas outlet 72.

Preferably, the exhaust port 72 may be communicated with the de-heaving tower heating furnace 14, the preliminary distillation tower heating furnace 25, the fluorene tower heating furnace 55, and the phenanthrene tower heating furnace 65, respectively. That is to say, collect the blow-down gas of each rectifying column top of the tower reflux drum, behind desulphurization unit 7 desorption hydrogen sulfide, get into each tower bottom heating furnace as the fuel gas, provide heat for each rectifying column after the burning, not only avoided the energy waste, practiced thrift the fuel, the cost is reduced, and final burning discharge after the blow-down gas desulfurization has reduced environmental pollution, has more security ring guarantor nature simultaneously.

The system for refining coal hydrogasification oil product provided by the embodiment has the advantages that:

(1) Heavy components are removed from the crude pyrene oil, energy waste caused by repeated heating of the heavy components is avoided, and heating and coking of the heavy components are prevented.

(2) Raw materials including crude pyrene oil, crude benzene oil and crude benzene are added into different rectifying towers in a grading manner, so that the components of oil products are effectively matched, and the phenomenon that the heat load is too high due to the fact that three oil products are added into the same rectifying tower at the same time, and the excessive waste heat is consumed is avoided.

(3) The fluorene oil, the phenanthrene oil and the pyrene-rich oil are extracted by adopting a continuous rectification mode, and the rectified product enters a buffer tank for storage, so that the method has the advantages of high production capacity, high automation level, low power consumption and the like compared with the batch rectification which is frequently adopted in the current industry.

(4) The fluorene oil on the top of the fluorene tower 5 and the phenanthrene oil on the top of the phenanthrene tower 6 can be used as heat sources of the benzene tower reboiler 46 and the naphthalene tower reboiler 34, so that the heat is effectively matched, and the energy is saved.

(5) The vent gas of the reflux tank at the top of the rectification tower is recycled and used as the fuel of the heating furnace after being desulfurized, so that the fuel is saved, the cost is reduced, and the environmental pollution is reduced.

(6) The fluorene oil, the phenanthrene oil and the pyrene-rich oil are subjected to melt crystallization treatment in a melt crystallization mode, so that compared with a solvent crystallization mode, the use of a solvent is avoided, equipment such as a centrifugal machine and a drying machine is reduced, and the method has the advantages of low cost and small pollution.

(7) The crystallized residual oil after the melting crystallization is returned to the rectifying tower, which is beneficial to recovering the product in the crystallized residual oil and improving the yield of the product.

(8) The process extracts high-added-value components such as refined benzene, refined naphthalene, refined fluorene, refined phenanthrene and refined pyrene at one time through coupling of different methods, has high product purity and yield and small device investment, greatly increases the overall economy of the coal hydro-gasification technology, and is suitable for industrial production.

The refining system carries out refining treatment on oil products produced by hydro-gasification, and sequentially carries out the steps of removing weight of crude pyrene oil, rectifying and extracting benzene and naphthalene, refining fluorene, phenanthrene and pyrene in a continuous rectification-crystallization mode, recycling vent gas and the like, so that high-added-value fine chemicals such as refined benzene, refined naphthalene, refined fluorene, refined phenanthrene and refined pyrene with the purity of more than 99% and the yield of more than 80% are obtained in a low-energy-consumption, low-cost and environment-friendly mode, the defect of low added value of the existing oil products is overcome, the hydro-gasification process is not only deeply extended, but also the added value of the oil products is greatly improved, and the economy and the competitiveness of the whole hydro-gasification technology are further improved.

The embodiment also provides a method for refining coal hydrogasification oil product, which can be partially or completely executed by the system for refining coal hydrogasification oil product provided by the embodiment to improve the added value of the oil product.

Referring to fig. 5, the method includes:

s101, introducing the crude pyrene oil into a de-heavy tower, and performing de-heavy treatment on the crude pyrene oil at a first preset pressure and a first preset temperature to obtain light pyrene oil on the top of the de-heavy tower.

S102, introducing the light pyrene oil and the crude benzene oil into a primary distillation tower, and rectifying the light pyrene oil and the crude benzene oil at a second preset temperature to obtain a light component oil product at the tower top of the primary distillation tower and obtain a heavy component oil product at the tower bottom of the primary distillation tower.

S103, introducing the light component oil into a naphthalene tower, and rectifying the light component oil at a third preset temperature to obtain benzene-rich fraction at the tower top of the naphthalene tower and refined naphthalene at the tower bottom of the naphthalene tower.

S104, introducing the benzene-rich fraction and the crude benzene into a benzene tower, and rectifying the benzene-rich fraction and the crude benzene at a fourth preset temperature to obtain refined benzene at the tower top of the benzene tower.

Wherein the toluene-rich component is obtained at the bottom of the benzene column, preferably, at least part of the toluene-rich component can be introduced into the naphthalene column, so that at least part of the toluene-rich component is rectified in the naphthalene column again.

The method for refining the oil product by using the refining system for the coal hydro-gasification oil product, provided by the embodiment, comprises the steps of firstly introducing crude pyrene oil into a heavy component removing tower, carrying out heavy component removing treatment on the crude pyrene oil through the heavy component removing tower to obtain light pyrene oil, then introducing the light pyrene oil and crude benzene oil into a primary distillation tower to carry out rectification treatment to obtain light component oil, then introducing the light component oil into a naphthalene tower to carry out rectification treatment to obtain refined naphthalene and benzene-rich fraction, and then introducing the benzene-rich fraction and the crude benzene into a benzene tower to carry out rectification treatment to obtain refined benzene. Meanwhile, the heavy component in the crude pyrene oil is prevented from being wasted by the repeated heating of a subsequent tower by performing the heavy component removing treatment on the crude pyrene oil, and the situation that the heavy component of the crude pyrene oil is excessively heated to cause viscosity increase and coking can be prevented. In addition, the crude pyrene oil, the crude benzene oil and the crude benzene are added into different towers in a grading manner for rectification, so that the components of the oil products are effectively matched, and the situation that the heat load is too high and too much ineffective heat is consumed due to the fact that three oil products are added into one tower for rectification at the same time is avoided.

Further, referring to fig. 6, after step S102, the method further includes:

s201, introducing at least part of heavy component oil into a fluorene tower, and rectifying the heavy component oil at a second preset pressure and a fifth preset temperature to obtain fluorene oil at the tower top of the fluorene tower and fluorene-removed oil at the tower bottom of the fluorene tower.

Specifically, at least part of the fluorene oil distilled from the top of the fluorene tower can be introduced into a benzene tower reboiler of the benzene tower, so that the fluorene oil exchanges heat in the benzene tower reboiler, and a heat source is provided for the benzene tower reboiler.

S202, carrying out melt crystallization treatment on the fluorene oil to obtain refined fluorene.

Specifically, the fluorene crystal residual oil obtained by performing melt crystallization treatment on the fluorene oil can be introduced into a fluorene tower and then rectified again, so as to further improve the collection rate of fluorene.

After step S201, the method further includes:

s203, introducing at least part of the defluorinated oil into a phenanthrene tower, and rectifying the defluorinated oil at a third preset pressure and a sixth preset temperature to obtain phenanthrene oil at the tower top of the phenanthrene tower and pyrene-rich oil at the tower bottom of the phenanthrene tower.

Specifically, at least part of phenanthrene oil distilled from the top of the phenanthrene tower is introduced into a naphthalene tower reboiler of the naphthalene tower, so that the phenanthrene oil exchanges heat in the naphthalene tower reboiler, and a heat source is provided for the naphthalene tower reboiler.

S204, carrying out melting crystallization treatment on the phenanthrene oil and the pyrene-rich oil to obtain refined phenanthrene and refined pyrene.

Wherein, can be with getting phenanthrene crystallization residual oil and pyrene crystallization residual oil that get after carrying out the melting crystallization processing to phenanthrene oil and rich pyrene oil and let in phenanthrene tower, carry out the rectification processing again to further improve the collection rate of phenanthrene and pyrene.

In a specific implementation, the method further comprises:

and the gas discharged from the heavy component removal tower reflux tank, the primary distillation tower reflux tank, the naphthalene tower reflux tank, the benzene tower reflux tank, the fluorene tower reflux tank and the phenanthrene tower reflux tank is subjected to desulfurization treatment by a desulfurization device. Further, the gas after desulfurization treatment can be introduced into a heavy component removal tower heating furnace, a primary distillation tower heating furnace, a fluorene tower heating furnace and a phenanthrene tower heating furnace.

The specific implementation manner and implementation principle are the same as those of the above embodiments, and can bring about the same or similar technical effects, and details are not repeated herein, and specific reference may be made to the description of the embodiment of the refining system.

It is noted that, in this document, relational terms such as "first" and "second," and the like, may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrases "comprising a," "8230," "8230," or "comprising" does not exclude the presence of additional like elements in a process, method, article, or apparatus that comprises the element.

The foregoing are merely exemplary embodiments of the present disclosure, which enable those skilled in the art to understand or practice the present disclosure. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the disclosure. Thus, the present disclosure is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A refining system of coal hydrogasification oil products is characterized by comprising a de-heavy tower (1), a primary distillation tower (2), a naphthalene tower (3) and a benzene tower (4);

the heavy pyrene removing tower (1) is provided with a crude pyrene oil inlet (11) for crude pyrene oil to enter the heavy pyrene removing tower, and the heavy pyrene removing tower (1) is used for removing heavy pyrene oil so as to obtain light pyrene oil at the tower top of the heavy pyrene removing tower (1);

the primary tower (2) is provided with a light pyrene oil inlet (21) and a crude benzene oil inlet (22) for crude benzene oil to enter the primary tower (2), the light pyrene oil inlet (21) is communicated with the top of the de-heavy tower (1) so that the light pyrene oil can enter the primary tower (2), the primary tower (2) is used for rectifying the light pyrene oil and the crude benzene oil so as to obtain light component oil products on the top of the primary tower (2), and heavy component oil products are obtained on the bottom of the primary tower (2);

the naphthalene tower (3) is provided with a light component oil product inlet (31) communicated with the top of the primary distillation tower (2), the light component oil product inlet (31) is used for allowing the light component oil product to enter the naphthalene tower (3), the naphthalene tower (3) is used for rectifying the light component oil product so as to obtain benzene-rich fraction at the top of the naphthalene tower (3) and obtain refined naphthalene at the bottom of the naphthalene tower (3);

the benzene tower (4) is provided with a benzene-rich fraction inlet (41) and a crude benzene inlet (42) for feeding crude benzene into the benzene tower (4), the benzene-rich fraction inlet (41) is communicated with the tower top of the naphthalene tower (3) for feeding the benzene-rich fraction into the benzene tower (4), and the benzene tower (4) is used for rectifying the benzene-rich fraction and the crude benzene to obtain refined benzene at the tower top of the benzene tower (4);

the refining system further comprises a fluorene tower (5), wherein the fluorene tower (5) is provided with a heavy component oil product inlet (51) communicated with the tower bottom of the primary distillation tower (2), the heavy component oil product inlet (51) is used for allowing heavy component oil products to enter the fluorene tower (5), the fluorene tower (5) is used for rectifying the heavy component oil products so as to obtain fluorene oil at the tower top of the fluorene tower (5) and obtain defluorinated oil at the tower bottom of the fluorene tower (5);

the refining system further comprises a phenanthrene tower (6), the phenanthrene tower (6) is provided with a fluorene removing oil inlet (61) communicated with the bottom of the fluorene tower (5), the fluorene removing oil inlet (61) is used for allowing the fluorene removing oil to enter the phenanthrene tower (6), the phenanthrene tower (6) is used for rectifying the fluorene removing oil so as to obtain phenanthrene oil on the top of the phenanthrene tower (6) and pyrene-rich oil on the bottom of the phenanthrene tower (6).

2. The refining system for coal hydrogasification oil product according to claim 1, further comprising a fluorene melt crystallizer (57);

the fluorene melt crystallizer (57) is provided with a fluorene oil pipeline (572) which is communicated with the top of the fluorene tower (5) and can be used for the fluorene oil to enter, and the fluorene melt crystallizer (57) is used for carrying out melt crystallization treatment on the fluorene oil so as to obtain refined fluorene.

3. The system for refining coal hydrogasification oil product according to claim 2, further comprising a phenanthrene melt crystallizer;

the phenanthrene melt crystallizer is provided with a phenanthrene oil pipeline which is communicated with the top of the phenanthrene tower (6) and can be used for the phenanthrene oil to enter, and the phenanthrene melt crystallizer is used for carrying out melt crystallization treatment on the phenanthrene oil so as to obtain fine phenanthrene.

4. The system for refining coal hydrogasification oil product according to claim 3, further comprising a pyrene melt crystallizer;

the pyrene melting crystallizer is provided with a pyrene-rich oil pipeline communicated with the bottom of the phenanthrene tower (6) and allowing the pyrene-rich oil to enter, and the pyrene melting crystallizer is used for carrying out melting crystallization treatment on the pyrene-rich oil to obtain refined pyrene.

5. The refining system of coal hydrogasification oil product according to claim 4, wherein the fluorene melt crystallizer (57) has a fluorene crystal residual oil discharge port (576), and the fluorene crystal residual oil discharge port (576) is communicated with the fluorene tower (5) so that fluorene crystal residual oil formed after the fluorene oil is subjected to melt crystallization treatment enters the fluorene tower (5);

the phenanthrene melting crystallizer is provided with a phenanthrene crystallization residual oil discharge port, the pyrene melting crystallizer is provided with a pyrene crystallization residual oil discharge port, and the phenanthrene crystallization residual oil discharge port and the pyrene crystallization residual oil discharge port are communicated with the phenanthrene tower (6), so that phenanthrene crystallization residual oil formed after the phenanthrene oil is subjected to melting crystallization treatment and pyrene crystallization residual oil formed after the pyrene-rich oil is subjected to melting crystallization treatment enter the phenanthrene tower (6).

6. The system for refining the coal hydrogasification oil product according to claim 3, wherein a benzene column reboiler (46) is provided at the bottom of the benzene column (4), and the top of the fluorene column (5) is communicated with the benzene column reboiler (46) so that the fluorene oil exchanges heat in the benzene column reboiler (46) to provide a heat source for the benzene column reboiler (46);

the bottom of the naphthalene tower (3) is provided with a naphthalene tower reboiler (34), and the top of the phenanthrene tower (6) is communicated with the naphthalene tower reboiler (34), so that the phenanthrene oil exchanges heat in the naphthalene tower reboiler (34) and a heat source is provided for the naphthalene tower reboiler (34).

7. The refining system of coal hydrogasification oil product according to any one of claims 1 to 6, wherein the bottom of the benzene column (4) is provided with a toluene-rich component discharge port (47), and the toluene-rich component discharge port (47) is communicated with the naphthalene column (3) so that at least part of the toluene-rich component formed at the bottom of the benzene column (4) enters the naphthalene column (3) for rectification treatment when the benzene column (4) is in rectification treatment.

8. The system for refining coal hydrogasification oil product according to any one of claims 3 to 6, further comprising a desulfurization device (7);

heavy tower reflux drum (13) of taking off of heavy tower (1), the first distillation column reflux drum (24) of first distillation column (2), naphthalene tower reflux drum (33) of naphthalene tower (3), benzene tower reflux drum (44) of benzene tower (4), fluorene tower reflux drum (53) of fluorene tower (5) and the rich and thin tower reflux drum (63) of rich and thin tower (6) all have gas discharge port, each gas discharge port all with desulphurization unit (7) intercommunication, desulphurization unit (7) are used for carrying out desulfurization treatment by each gas discharge port combustion gas, desulphurization unit (7) have gas vent (72), gas vent (72) respectively with heavy tower heating furnace (14) of taking off of heavy tower (1), first distillation column heating furnace (25) of first distillation column (2), fluorene tower heating furnace (55) of fluorene tower (5) and rich and thin tower heating furnace (65) intercommunication of rich and thin tower (6).

9. A method for refining oil products by using the system for refining coal hydrogasification oil products according to any one of claims 1 to 8, wherein the method comprises the following steps:

introducing the light pyrene oil and the crude benzene oil into a primary distillation tower, and rectifying the light pyrene oil and the crude benzene oil at a second preset temperature to obtain a light component oil at the tower top of the primary distillation tower and obtain a heavy component oil at the tower bottom of the primary distillation tower;

introducing the benzene-rich fraction and the crude benzene into a benzene tower, and rectifying the benzene-rich fraction and the crude benzene at a fourth preset temperature to obtain refined benzene at the tower top of the benzene tower;

the method comprises the following steps of introducing the light pyrene oil and the crude benzene oil into a primary distillation tower, rectifying the light pyrene oil and the crude benzene oil at a second preset temperature to obtain a light component oil product at the tower top of the primary distillation tower, and obtaining a heavy component oil product at the tower bottom of the primary distillation tower, wherein the method further comprises the following steps:

introducing at least part of the heavy component oil into a fluorene tower, and rectifying the heavy component oil at a second preset pressure and a fifth preset temperature to obtain fluorene oil at the tower top of the fluorene tower and defluorinated oil at the tower bottom of the fluorene tower;

introducing at least part of the defluorinated oil into a phenanthrene tower, and rectifying the defluorinated oil under a third preset pressure and a sixth preset temperature to obtain phenanthrene oil at the tower top of the phenanthrene tower and pyrene-rich oil at the tower bottom of the phenanthrene tower.

10. The method as claimed in claim 9, wherein the step of introducing at least part of the heavy component oil into the fluorene tower, rectifying the heavy component oil at a second preset pressure and a fifth preset temperature to obtain the fluorene oil at the top of the fluorene tower, and after the step of obtaining the defluorinated oil at the bottom of the fluorene tower, the method further comprises:

11. The method as claimed in claim 10, wherein the step of introducing at least part of the heavy component oil into the fluorene tower, rectifying the heavy component oil at a fifth preset temperature to obtain fluorene oil at the top of the fluorene tower, and obtaining the defluorinated oil at the bottom of the fluorene tower is followed by the step of:

and carrying out melting crystallization treatment on the phenanthrene oil and the pyrene-rich oil to obtain refined phenanthrene and refined pyrene.

12. The method of claim 11, further comprising:

introducing fluorene crystal residual oil obtained by carrying out melt crystallization treatment on the fluorene oil into the fluorene tower;

13. The method of claim 11, further comprising:

and introducing at least part of the phenanthrene oil into a naphthalene tower reboiler, so that the phenanthrene oil exchanges heat in the naphthalene tower reboiler, and a heat source is provided for the naphthalene tower reboiler.

14. The method according to any one of claims 9 to 13, wherein after the step of introducing the benzene-rich fraction and the crude benzene into the benzene column and subjecting the benzene-rich fraction and the crude benzene to a rectification treatment at a fourth preset temperature to obtain refined benzene at the top of the benzene column, the method further comprises:

passing at least a portion of the toluene-rich component formed at the bottom of the benzene column to the naphthalene column to subject the at least a portion of the toluene-rich component to a rectification process in the naphthalene column.

15. The method according to any one of claims 11 to 13, further comprising:

carrying out desulfurization treatment on gas discharged from a heavy component removal tower reflux tank, a primary distillation tower reflux tank, a naphthalene tower reflux tank, a benzene tower reflux tank, a fluorene tower reflux tank and a phenanthrene tower reflux tank by a desulfurization device;