CN218755605U

CN218755605U - Coal tar hydrocracking system

Info

Publication number: CN218755605U
Application number: CN202222877838.1U
Authority: CN
Inventors: 司传煜; 崔联涛; 张美荣; 陈克垒; 郭道军; 满建文; 周腾
Original assignee: Shandong Hengxin Technology Development Co ltd
Current assignee: Shandong Hengxin Technology Development Co ltd
Priority date: 2022-10-31
Filing date: 2022-10-31
Publication date: 2023-03-28
Anticipated expiration: 2032-10-31

Abstract

The utility model relates to a hydrocracking unit field, concretely relates to coal tar hydrocracking system. The method comprises the following steps: the device comprises a hydrogenation unit, a separation unit, a cracking unit, a hydrogen circulation unit and a fractionation device; the hydrogenation unit comprises a first hydrofining reactor, a second hydrofining reactor, a third hydrofining reactor, a fourth hydrofining reactor and a fifth hydrofining reactor which are connected in series in sequence; the separation unit comprises a hot high-pressure separator, a cold high-pressure separator and a cold low-pressure separator; the cracking unit comprises a first cracking reactor and a second cracking reactor which are connected in series; a discharge pipeline of the fifth hydrogen refining reactor is connected to a hot high-pressure separator, a hot high-pressure oil discharge pipeline of the hot high-pressure separator is connected to the first cracking reactor, a hot high-pressure gas discharge pipeline is connected to a cold high-pressure separator, a cold high-pressure gas discharge pipeline of the cold high-pressure separator is connected to the first cracking reactor, a cold high-pressure oil discharge pipeline is connected to a cold low-pressure separator, and a cold low-oil discharge pipeline of the cold low-pressure separator is connected to a fractionation device; the discharge pipeline of the second cracking reactor is connected to a fractionation device; the hydrogen recycle unit is used for providing hydrogen for the hydrogenation unit and the cracking unit.

Description

Coal tar hydrocracking system

Technical Field

The utility model relates to a hydrocracking unit field, concretely relates to coal tar hydrocracking system.

Background

The coal tar hydrocracking process in the prior art comprises the following steps: the coal tar is subjected to reduced pressure fractionation to become light anthracene oil and heavy anthracene oil, the light and heavy anthracene oil enters a hydrofining reactor and then enters a hot high-pressure separator, and a low-oil-separation phase and a gas phase are obtained after passing through the separator: part of the light oil and the gas phase are communicated with a cold high-pressure separator and a cold low-pressure separator, and the obtained cold low-fraction oil and the cold low-pressure separator oil phase are sent to an absorption stabilizing part, and are sent to a hydrocracking reactor after part of sulfur is removed through absorption stabilizing; the other part of the oil phase is sent directly to hydrocracking. And carrying out vacuum fractionation after a hydrocracking process to obtain a product. The disadvantages are that: compared with the thermal separation oil, the light oil phase high-gas-separation condensed oil after hydrofining has low density and few components, if the condensed oil is subjected to hydrocracking, the oil is deeply cracked, the final product is easy to generate liquefied gas, and the yield of the product oil is reduced.

SUMMERY OF THE UTILITY MODEL

The utility model discloses the technical problem that will solve is:

aiming at the defects of more liquefied gas and low yield of product oil produced by the coal tar hydrocracking system in the prior art, the coal tar hydrocracking system capable of improving the yield of the product oil is provided.

The utility model provides an above-mentioned technical problem's technical scheme as follows:

a coal tar hydrocracking system is characterized by comprising: the device comprises a hydrogenation unit, a separation unit, a cracking unit, a hydrogen circulation unit and a fractionation device; the hydrogenation unit comprises a first hydrofining reactor, a second hydrofining reactor, a third hydrofining reactor, a fourth hydrofining reactor and a fifth hydrofining reactor which are connected in series in sequence; the separation unit comprises a hot high-pressure separator, a cold high-pressure separator and a cold low-pressure separator; the cracking unit comprises a first cracking reactor and a second cracking reactor which are connected in series; a discharge pipeline of the fifth hydrogen refining reactor is connected to a hot high-pressure separator, a hot high-pressure oil discharge pipeline of the hot high-pressure separator is connected to the first cracking reactor, a hot high-pressure gas discharge pipeline is connected to a cold high-pressure separator, a cold high-pressure gas discharge pipeline of the cold high-pressure separator is connected to the first cracking reactor, a cold high-pressure oil discharge pipeline is connected to a cold low-pressure separator, and a cold low-oil discharge pipeline of the cold low-pressure separator is connected to a fractionation device; the discharge pipeline of the second cracking reactor is connected to a fractionation device; the hydrogen circulation unit is used for providing hydrogen for the hydrogenation unit and the cracking unit.

Preferably, at least one layer of protective agent bed layer is arranged in the first hydrofining reactor, the upper layer in the second hydrofining reactor is provided with a protective agent bed layer, the lower layer is provided with a mixed bed layer of a protective agent and a hydrogenation catalyst, and at least three layers of hydrogenation catalysts are arranged in the third hydrofining reactor, the fourth hydrofining reactor and the fifth hydrofining reactor.

Preferably, the mixed bed layer further comprises active ceramic balls and inert ceramic balls, and the protective agent, the inert ceramic balls, the active ceramic balls and the hydrogenation catalyst are sequentially filled in the mixed bed layer from top to bottom.

Preferably, the upper end of the first hydrofining reactor is provided with a light anthracene oil inlet, and the upper end of the second hydrofining reactor is provided with a heavy anthracene oil inlet.

Preferably, light anthracene oil entrance is connected with light anthracene oil feed line, light anthracene oil feed line is including the light anthracene oil tank, light anthracene oil filter, light anthracene oil buffer tank, light anthracene oil booster pump and the heat exchanger that connect gradually, and the heat exchanger is connected on light anthracene oil entrance.

Preferably, heavy anthracene oil inlet is connected with heavy anthracene oil feed line, heavy anthracene oil feed line is including the heavy anthracene oil tank, heavy anthracene oil filter, heavy anthracene oil buffer tank and the heavy anthracene oil booster pump that connect gradually, and heavy anthracene oil booster pump is connected on heavy anthracene oil inlet.

The utility model has the advantages that:

the utility model discloses a set up the hydrogenation unit and include five refined reactors, and the configuration is rationally loaded to protective agent and hydrogenation catalyst, and the cold low oil discharge tube who sets up cold low pressure separator is connected to the fractionating device, the realization has improved the throughput of hydrogenation unit, make partial heavy oil just can the hydrogenation decompose into the light oil in refined reactor, thereby reduce cold low oil density, cold low oil can directly be sent to the fractionating device and fractionate and obtain the product, no longer through absorbing stable and hydrocracking reactor, furthest's the production that reduces the liquefied gas, thereby improve product oil yield.

Drawings

Fig. 1 is a schematic structural diagram of the present invention;

in the figure: 1. a hydrogenation unit, 2 a separation unit, 3 a cracking unit, 4 a hydrogen circulation unit, 5 a fractionation device, 10 a first hydrofining reactor, 11, a second hydrofining reactor, 12, a third hydrofining reactor, 13, a fourth hydrofining reactor, 14, a fifth hydrofining reactor; 20. hot high-pressure separator, 21 cold high-pressure separator, 22 cold low-pressure separator; 30. a first cracking reactor, 31, a second cracking reactor.

Detailed Description

The principles and features of the present invention will be described with reference to the drawings, which are provided for illustration only and are not intended to limit the scope of the invention.

As shown in fig. 1, the coal tar hydrocracking system of the embodiment includes: a hydrogenation unit 1, a separation unit 2, a cracking unit 3, a hydrogen recycle unit 4 and a fractionation unit 5. The hydrogen recycle unit 4 is used to provide hydrogen to the hydrogenation unit 1 and the cracking unit 3.

The hydrogenation unit 1 comprises a first hydrofining reactor 10, a second hydrofining reactor 11, a third hydrofining reactor 12, a fourth hydrofining reactor 13 and a fifth hydrofining reactor 14 which are connected in series in sequence; preferably, the upper end of the first hydrofining reactor 10 is provided with a light anthracene oil inlet, and the upper end of the second hydrofining reactor 11 is provided with a heavy anthracene oil inlet.

Light anthracene oil entrance is connected with light anthracene oil feed line, light anthracene oil feed line is including the light anthracene oil tank, light anthracene oil filter, light anthracene oil buffer tank, light anthracene oil booster pump and the heat exchanger that connect gradually, and the heat exchanger is connected on light anthracene oil entrance.

Heavy anthracene oil entrance is connected with heavy anthracene oil feed line, heavy anthracene oil feed line is including the heavy anthracene oil tank, heavy anthracene oil filter, heavy anthracene oil buffer tank and the heavy anthracene oil booster pump that connect gradually, and heavy anthracene oil booster pump is connected on heavy anthracene oil entrance.

At least one bed layer of the protective agent is arranged in the first hydrofining reactor 10, preferably, four bed layers are arranged in the first hydrofining reactor 10, the protective agent and the seven-hole balls are filled in the first bed layer at the uppermost end, the protective agent and the transition agent are filled in the second bed layer, and the transition agent is filled in the third bed layer and the fourth bed layer.

The upper layer in the second hydrorefining reactor 11 is provided with a protective agent bed layer, and the lower layer is provided with a mixed bed layer of a protective agent and a hydrogenation catalyst. Specifically, the mixed bed layer further comprises active ceramic balls and inert ceramic balls, and a protective agent, the inert ceramic balls, the active ceramic balls and a hydrogenation catalyst are sequentially filled in the mixed bed layer from top to bottom.

At least three layers of hydrogenation catalysts are arranged in the third hydrogenation refining reactor 12, the fourth hydrogenation refining reactor 13 and the fifth hydrogenation refining reactor 14.

The separation unit 2 comprises a hot high-pressure separator 20, a cold high-pressure separator 21 and a cold low-pressure separator 22.

The cracking unit 3 comprises a first cracking reactor 30 and a second cracking reactor 31 connected in series.

A discharge pipeline of the fifth hydrogen refining reactor 14 is connected to the hot high-pressure separator 20, a hot high-fraction oil discharge pipeline of the hot high-pressure separator 20 is connected to the first cracking reactor 30, a hot high-fraction gas discharge pipeline is connected to the cold high-pressure separator 21, a cold high-fraction gas discharge pipeline of the cold high-pressure separator 21 is connected to the first cracking reactor 30, a cold high-fraction oil discharge pipeline is connected to the cold low-pressure separator 22, and a cold low-oil discharge pipeline of the cold low-pressure separator 22 is connected to the fractionating device 5; the discharge conduit of the second cracking reactor 31 is connected to a fractionation unit 5.

The utility model discloses a set up hydrogenation unit 1 and include five refined reactors, and protective agent and hydrogenation catalyst have carried out reasonable configuration of loading. The protective agent is mainly used for hydrolyzing organic iron in the raw material to convert the organic iron into iron sulfide and depositing the iron sulfide in a pore channel, so that metal impurities and solid particles in an oil product can be effectively removed, and a substance which is easy to coke in the raw material is properly hydrogenated, so that the poisoning and coking of the catalyst are slowed down, the service life of the catalyst is prolonged, and the aims of protecting hydrofining and hydrocracking are fulfilled. The device is provided with the protective agents in the first hydrofining reactor 10 and the second hydrofining reactor 11, the total amount of the protective agents is large, the capability of removing metals and particulate matters in raw oil is strong, the influence of metal ions on the activity of the catalyst is effectively reduced, the reaction depth of the catalyst is improved, part of heavy oil can be hydrogenated and decomposed into light oil in the refining reactors, and the purpose of reducing the density of cold low oil is achieved.

It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications can be made without departing from the scope of the invention.

Claims

1. A coal tar hydrocracking system, characterized by comprising: a hydrogenation unit (1), a separation unit (2), a cracking unit (3), a hydrogen circulation unit (4) and a fractionation device (5); the hydrogenation unit (1) comprises a first hydrofining reactor (10), a second hydrofining reactor (11), a third hydrofining reactor (12), a fourth hydrofining reactor (13) and a fifth hydrofining reactor (14) which are sequentially connected in series; the separation unit (2) comprises a hot high-pressure separator (20), a cold high-pressure separator (21) and a cold low-pressure separator (22); the cracking unit (3) comprises a first cracking reactor (30) and a second cracking reactor (31) connected in series; a discharge pipeline of the fifth hydrogen refining reactor (14) is connected to the hot high-pressure separator (20), a hot high-pressure oil discharge pipeline of the hot high-pressure separator (20) is connected to the first cracking reactor (30), a hot high-pressure gas discharge pipeline is connected to the cold high-pressure separator (21), a cold high-pressure gas discharge pipeline of the cold high-pressure separator (21) is connected to the first cracking reactor (30), a cold high-pressure oil discharge pipeline is connected to the cold low-pressure separator (22), and a cold low-oil discharge pipeline of the cold low-pressure separator (22) is connected to the fractionating device (5); the discharge pipeline of the second cracking reactor (31) is connected to the fractionating device (5); the hydrogen recycling unit (4) is used for supplying hydrogen to the hydrogenation unit (1) and the cracking unit (3).

2. The coal tar hydrocracking system according to claim 1, wherein at least one layer of protective agent bed layer is arranged in the first hydrofining reactor (10), the upper layer of the second hydrofining reactor (11) is provided with a protective agent bed layer, the lower layer of the second hydrofining reactor is provided with a mixed bed layer of a protective agent and a hydrogenation catalyst, and at least three layers of hydrogenation catalysts are arranged in the third hydrofining reactor (12), the fourth hydrofining reactor (13) and the fifth hydrofining reactor (14).

3. The coal tar hydrocracking system of claim 2, wherein the mixed bed further comprises active ceramic balls and inert ceramic balls, and the protective agent, the inert ceramic balls, the active ceramic balls and the hydrogenation catalyst are sequentially filled in the mixed bed from top to bottom.

4. The coal tar hydrocracking system according to any one of claims 1 to 3, wherein a light anthracene oil inlet is formed at the upper end of the first hydrofining reactor (10), and a heavy anthracene oil inlet is formed at the upper end of the second hydrofining reactor (11).

5. The coal tar hydrocracking system of claim 4, wherein a light anthracene oil feed line is connected to the light anthracene oil inlet, the light anthracene oil feed line comprises a light anthracene oil tank, a light anthracene oil filter, a light anthracene oil buffer tank, a light anthracene oil booster pump and a heat exchanger which are connected in sequence, and the heat exchanger is connected to the light anthracene oil inlet.

6. The coal tar hydrocracking system of claim 4, wherein a heavy anthracene oil feeding pipeline is connected to the heavy anthracene oil inlet, and the heavy anthracene oil feeding pipeline comprises a heavy anthracene oil tank, a heavy anthracene oil filter, a heavy anthracene oil buffer tank and a heavy anthracene oil booster pump which are connected in sequence, and the heavy anthracene oil booster pump is connected to the heavy anthracene oil inlet.