CN110408433A - A kind of method of coal tar production needle coke and BTX - Google Patents

A kind of method of coal tar production needle coke and BTX Download PDF

Info

Publication number
CN110408433A
CN110408433A CN201810391509.1A CN201810391509A CN110408433A CN 110408433 A CN110408433 A CN 110408433A CN 201810391509 A CN201810391509 A CN 201810391509A CN 110408433 A CN110408433 A CN 110408433A
Authority
CN
China
Prior art keywords
coal tar
hydrogen
fraction
catalyst
hydrogenation
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN201810391509.1A
Other languages
Chinese (zh)
Other versions
CN110408433B (en
Inventor
梁家林
吴昊
李猛
戴立顺
胡志海
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sinopec Research Institute of Petroleum Processing
China Petrochemical Corp
Original Assignee
Sinopec Research Institute of Petroleum Processing
China Petrochemical Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Sinopec Research Institute of Petroleum Processing, China Petrochemical Corp filed Critical Sinopec Research Institute of Petroleum Processing
Priority to CN201810391509.1A priority Critical patent/CN110408433B/en
Publication of CN110408433A publication Critical patent/CN110408433A/en
Application granted granted Critical
Publication of CN110408433B publication Critical patent/CN110408433B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/06—Catalytic processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The present invention relates to coal chemical technologies, the method for a kind of coal tar production needle coke and BTX are disclosed, this method comprises: full fraction of coal tar is cut into coal tar light component and coal tar heavy duty component；Coal tar light component enters the first hydrogenation unit and is reacted, the clarified oil of coal tar heavy duty component enters the second hydrogenation unit and is reacted, obtain the raw material of production needle coke, needle coke product is made by delayed coking and calcine technology again, the coal tar light component rich in BTX obtains BTX product by Aromatics Extractive Project.Using method of the invention, thermal expansion coefficient low needle coke product and BTX industrial chemicals can be produced.

Description

A kind of method of coal tar production needle coke and BTX
Technical field
The present invention relates to coal chemical technologies, and in particular, to a kind of full fraction of coal tar raw material production needle coke and BTX's Method.
Background technique
Coal is the important fossil energy in China, is accounted in China's non-renewable energy consumption result relatively high.China experienced 30 years rapid economic developments, the consumption of coal resources also increase rapidly.In recent years, China's economic growth rate is gradually Reduce, and will the long-term growth rate for maintaining high speed, the following industrial transformation upgrading by be China's economy face one A problem.Cleaning, environmental protection and it is efficient using coal resources by be coal in China industry development inexorable trend.Coal classification benefit With being developing direction that China vigorously advocated in recent years, objective is efficiently to utilize coal resources.The pass of coal classified utilization Key link is pyrolysis and the subsequent product processing scheme of coal, and wherein the coai-tar product deep processing of coal pyrolysis produces high value Product is one of the core technology of coal classified utilization.
Currently, coal tar is mainly for the production of large transportation fuel such as petrol and diesel oil, it is long-term however as oil price 40~60 U.S. dollars/bucket is maintained, the processing scheme for producing transportation fuel by coal tar hydrogenating is economical increasingly to be reduced, special It is not to be maintained essentially on break even line with the processing scheme of coal tar cutting fraction production petrol and diesel oil product.Therefore, pass through Coal tar production higher value product is the committed step of coal classified utilization.
Needle coke is the raw material for manufacturing high power and ultra-high power graphite electrode, is had using graphite electrode prepared by needle coke The advantages that thermal expansion coefficient is low, high mechanical strength, small oxidation susceptibility, currently, needle coke is divided into petroleum base according to the difference of raw material Needle coke and coal-based needle are burnt, and petroleum-based needle coke is using residual oil or catalytic cracked oil pulp as raw material, and coal-based needle coke is with coal tar Double distilled be divided into raw material.The needle coke that the country is able to produce at present is petroleum-based needle coke, and the production of coal-based needle coke is not yet It appears in the newspapers.The country has had been provided with the technology using needle coke production high power electrodes, but there is still a need for a large amount of for needle-shape coke raw material Import.Therefore, producing needle coke by coal tar has biggish market prospects.
It is produced currently, the progress hydrogenation technique processing of middle coalite tar is prepared diesel oil by domestic coal tar processing corporate boss Product and a small amount of naphtha product, diesel product have faced the situation that supply exceed demand, therefore the warp of this processing technology at home Ji property is poor.The heavy constituent of middle coalite tar is and unprocessed because having the characteristics that residual carbon content is high, asphaltene colloid content Middle coalite tar heavy constituent cannot be directly as the raw material of production needle coke, general enterprises be difficult have suitable process This part heavy constituent.
CN103013566A discloses a kind of technique using coal tar asphalt production needle-shape coke raw material, and the technique is by pitch Most of quinoline insolubles in asphalt stock are removed after being sufficiently mixed with solvent, and the pitch of low quinoline insolubles is being carried out to add hydrogen Thermal decomposition prepares the raw material of needle coke to acquisition.Solvent in this method is the aromatic mixture of BTX or coal base.The party Method fails organically to tie and the product property feature after coal tar light fraction working process.
CN103509572A discloses a kind of technique using using solvent method preparation high-quality coal-based needle coke, the technique Solvent insolubles are removed using the method for physical separation after coal measures raw material and solvent are mixed evenly and obtain clarified solution, wherein Solvent include hydro carbons that 200 DEG C~350 DEG C fraction sections of coal tar or coal tar fraction add 200 DEG C~300 DEG C fractions after hydrogen.It should Method underuses the property feature production of coal tar light fraction using the coal tar fraction section rich in aromatic hydrocarbons as solvent High-value product.
CN101538482B discloses a kind of middle coalite tar deep working method, and this method locates middle coalite tar in advance It is fractionated to obtain light fraction, carbolic oil and heavy distillat after reason, heavy distillat carries out coking and handles to obtain coking gasoline and diesel, coking vapour bavin Oil mixes the naphtha being hydrocracked as hydrofinishing and the raw material being hydrocracked with light fraction as catalytic reforming Raw material carries out aromatic hydrocarbons drawer after catalytic reforming and obtains the industrial chemicals such as BTX.This method process is complicated, and fails to make full use of coal Heavy distillat in tar, therefore the economy of technique is poor.
CN106782979A discloses the technique that coalite tar and hard pitch prepare needle coke in a kind of utilization.The work The heavy distillat for being greater than 350 DEG C in middle coalite tar is carried out hydropyrolysis reaction by skill, and the heavy constituent of generation is by centrifuge separation Obtained heavy distillat can be used as the raw material of production needle coke.The technique reduces the quinoline non-soluble in raw material by hydrogenation reaction The heavy distillat of object, plant investment higher cost, and hydrogenation reaction needs to remove consolidating in heavy distillat by the method for centrifuge separation Body catalyst, complex process, and underuse the light component of middle coalite tar.
Summary of the invention
The object of the present invention is to provide a kind of full fraction of coal tar raw material production needle coke and BTX (benzene,toluene,xylene) Method.
To achieve the goals above, this method comprises:
A kind of method of coal tar production needle coke and BTX, this method comprises:
(1) full fraction of coal tar raw material after pretreatment, is cut into coal tar light component and coal tar heavy duty component, coal tar The cut point of light component and coal tar heavy duty component is 350 DEG C~400 DEG C；
(2) coal tar light component enters the first hydrogenation unit, contacts and is reacted with hydrocracking catalyst, reaction stream Object obtains adding hydrogen light naphthar plus hydrogen heavy naphtha and hydrogenated diesel oil after separation and fractionation out；
(3) the resulting coal tar heavy duty component of step (1) adds hydrogen heavy naphtha to be mixed with obtained by step (2), obtains clear Clear liquid and insoluble matter；
(4) clarified solution obtained by step (3) obtains fraction I and fraction II through separation process；
(5) fraction II obtained by step (4) is the coal tar heavy duty component containing low quinoline insolubles, and fraction II enters second plus hydrogen Unit is contacted with hydrogenation catalyst and is reacted under hydrogenation conditions, and reaction effluent obtains after separation and fractionation To hydrogen coal tar asphalt is added, the described plus delayed coking of hydrogen coal tar asphalt and calcination process obtain needle coke product；
(6) the fraction I that step (3) obtains is the coal tar light component rich in BTX, and the fraction I is obtained after Aromatics Extractive Project To BTX product.
Method provided by the invention makes full use of light component and heavy constituent in conjunction with the molecule feature of coal tar different component Middle composition converts the aromatic hydrocarbons in coal tar light component to the BTX product of high value, and will be polycyclic in coal tar heavy duty component Aromatic component is converted into the needle coke product of high value, realizes that the utilization efficiency of full fraction of coal tar raw material maximizes and economy is imitated Benefit maximizes.
Specific embodiment
Detailed description of the preferred embodiments below.It should be understood that described herein specific Embodiment is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
The endpoint of disclosed range and any value are not limited to the accurate range or value herein, these ranges or Value should be understood as comprising the value close to these ranges or value.For numberical range, between the endpoint value of each range, respectively It can be combined with each other between the endpoint value of a range and individual point value, and individually between point value and obtain one or more New numberical range, these numberical ranges should be considered as specific open herein.
The object of the present invention is to provide it is a kind of by full fraction of coal tar produce the chemical industry material such as needle coke and BTX technique, This method comprises:
(1) full fraction of coal tar raw material after pretreatment, is cut into coal tar light component and coal tar heavy duty component, coal tar The cut point of light component and coal tar heavy duty component is 350 DEG C~400 DEG C；
(2) coal tar light component enters the first hydrogenation unit, contacts and is reacted with hydrocracking catalyst, reaction stream Object obtains adding hydrogen light naphthar plus hydrogen heavy naphtha and hydrogenated diesel oil after separation and fractionation out；
(3) the resulting coal tar heavy duty component of step (1) adds hydrogen heavy naphtha to be mixed with obtained by step (2), obtains clear Clear liquid and insoluble matter；
(4) clarified solution obtained by step (3) obtains fraction I and fraction II through separation process；
(5) fraction II obtained by step (4) is the coal tar heavy duty component containing low quinoline insolubles, and fraction II enters second plus hydrogen Unit is contacted with hydrogenation catalyst and is reacted under hydrogenation conditions, and reaction effluent obtains after separation and fractionation To hydrogen coal tar asphalt is added, the described plus delayed coking of hydrogen coal tar asphalt and calcination process obtain needle coke product；
(6) the fraction I that step (3) obtains is the coal tar light component rich in BTX, and the fraction I is obtained after Aromatics Extractive Project To BTX product.
In the present invention, the preprocessing process of full fraction of coal tar raw material includes but is not limited to boiling bed hydrogenation process, slurry Bed hydroprocessing process or other preprocessing process, main purpose are most of metal, the ash contents removed in full fraction of coal tar raw material Equal impurity.It is preferred that tenor is less than 50 μ g/g, and water content is less than 300 μ in full fraction of coal tar raw material after pretreatment G/g, content of ashes is less than 0.01 weight %.
In the present invention, full fraction of coal tar raw material after pretreatment, is cut into coal tar light component and coal tar heavy duty component, The cut point of the preferred coal tar light component and coal tar heavy duty component is 360 DEG C~390 DEG C.
In the one of embodiment of the present invention, the first hydrogenation unit is fixed bed hydrogenation Cracking Unit or slurry bed hydroprocessing Cracking Unit or boiling bed hydrogenation Cracking Unit.The reaction condition of first hydrogenation unit includes: that reaction pressure is 6~30MPa, instead Answering temperature is 320~490 DEG C, and volume space velocity is 0.1~5.0h when liquid-1, hydrogen to oil volume ratio is 200~2000.
In the present invention, the first hydrogenation unit is preferably fixed bed hydrogenation Cracking Unit.The fixed bed hydrogenation cracking list Member is one-part form fixed bed hydrogenation cracking process or is two-part fixed bed hydrogenation cracking process.It is preferred that the fixed bed hydrogenation The reaction condition of Cracking Unit includes: that reaction pressure is 10~13MPa, and reaction temperature is 350~410 DEG C, volume space velocity when liquid For 0.5~2.0h-1, hydrogen to oil volume ratio is 800~1500.
Preferably, Hydrobon catalyst and hydrocracking catalyst are loaded in the fixed bed hydrogenation Cracking Unit, with The filling ratio of stereometer, Hydrobon catalyst and hydrocracking catalyst is 2:8~8:2.Coal tar light component and plus hydrogen The hetero atoms such as sulphur, nitrogen, the metal in coal tar light component are removed after catalyst for refining contact, and are saturated part aromatic hydrocarbons.Then, with Hydrocracking catalyst contact carries out hydrocracking reaction, generates dry gas, liquefied gas plus hydrogen light naphthar plus hydrogen heavy naphtha And hydrogenated diesel oil.
Preferably, the active metal member in the Hydrobon catalyst containing carrier and load on the carrier Element, the carrier are selected from least one of aluminium oxide, aluminium oxide-silicon oxide and titanium oxide, and the active metallic element is selected from At least one of nickel, cobalt, molybdenum and tungsten；It is further preferred that in Hydrobon catalyst, with the total of Hydrobon catalyst The content of poidometer, nickel and/or cobalt in terms of oxide is 1~30 weight %, and the content of molybdenum and/or tungsten in terms of oxide is 5~35 weight %.
Preferably, the active metal member in the hydrocracking catalyst containing carrier and load on the carrier Element, the carrier contain molecular sieve and selected from least one of aluminium oxide, aluminium oxide-silicon oxide and titanium oxide, the activity Metallic element is selected from least one of nickel, cobalt, molybdenum and tungsten；The heap density of the hydrocracking catalyst is 0.4~1.3g/ cm3, hydrocracking catalyst average grain diameter is 0.08~1.2mm, and specific surface area is 100~300m2/g；Further preferably Ground, in hydrocracking catalyst, with the total weight of hydrocracking catalyst, molecular sieve content is 10~60 weight %, with The nickel of oxide meter and/or the content of cobalt are 1~30%, and the content of molybdenum and/or tungsten in terms of oxide is 5~40 weight %.
In the present invention, the first hydrogenation unit reaction effluent of step (2) obtains after separation and fractionation plus hydrogen pumice brain Oil plus hydrogen heavy naphtha and hydrogenated diesel oil, it is preferable that add hydrogen light naphthar and the cut point between hydrogen heavy naphtha is added to be 60~85 DEG C, adding the cut point between hydrogen heavy naphtha and hydrogenated diesel oil is 175~190 DEG C；Wherein, the yield for adding hydrogen light naphthar is 10 ~20%, adding the yield of hydrogen heavy naphtha is 15~70%, and hydrogenated diesel oil yield is 5~60%.
Preferably, hydrogenated diesel oil is recycled to the first hydrogenation unit entrance and continues to react, and further generates and adds hydrogen scheelite Cerebrol.
In step of the present invention (3), hydrogen scheelite brain will be added obtained by the resulting coal tar heavy duty component of step (1) and step (2) Oil is mixed, and clarified solution and insoluble matter are obtained.Wherein the predominant amount of insoluble matter is quinoline insolubles.It is preferred that coal tar heavy duty Component is 0.1~10 with the mass ratio for adding hydrogen heavy naphtha, and preferred mass ratio is 2~5.
Preferably, in step (3) coal tar heavy duty component with plus hydrogen heavy naphtha mix when temperature be 40 DEG C~120 DEG C, More preferably 60 DEG C~90 DEG C.
In step of the present invention (4), clarified solution obtained by step (3) obtains fraction I and fraction II through separation process.It is preferred that Separation process described in step (4) is physical partition method, and the physical partition method includes the separation such as the way of distillation and centrifugal separation Method, further preferably centrifugal separation.
In the present invention, gained fraction II is the coal tar heavy duty component containing low quinoline insolubles, and fraction II enters second and adds Hydrogen unit is contacted with hydrogenation catalyst and is reacted under hydrogenation conditions.
Preferably, the hydrogenation catalyst is Fe-series catalyst, more preferably vulcanization iron powder.
Preferably, the mass ratio 0.1~3% of hydrogenation catalyst and fraction II, preferred mass ratio be 0.005~ 0.015。
Preferably, auxiliary agent is contained in the Fe-series catalyst, auxiliary agent is oil-soluble CoO and/or MoO3, auxiliary agent and fraction The mass ratio of II is 0.001~0.02, and preferred mass ratio is 0.005~0.008.
Preferably, in step (5) hydrogenation conditions include: reaction temperature be 350~450 DEG C, hydrogen partial pressure be 4.5~ 13.0MPa, hydrogen-oil ratio are 300~1500.
In the present invention, the described plus delayed coking of hydrogen coal tar asphalt and calcination process obtain needle coke product；Described Delayed coking and calcination process are the technical process of conventional production needle coke.
In the present invention, the fraction I that step (3) obtains is the coal tar light component rich in BTX, and the fraction I takes out through aromatic hydrocarbons BTX product is obtained after mentioning.The Aromatics Extractive Project is conventional aromatics extraction process.
The present invention will be further described through by embodiment below, but not thereby limiting the invention.
Embodiment 1
The full feedstock of middle coalite tar is pre-processed, the property of the middle full fraction of coalite tar is shown in Table 1.Through pre- In treated full fraction of coal tar raw material, tenor is 20 μ g/g, and 200 μ g/g of water content, content of ashes is 0.005 weight Measure %.Full fraction of coal tar raw material after pretreatment is cut into coal tar light component and coal tar heavy duty component by fractionating column, The cut point of coal tar light component and coal tar heavy duty component is 380 DEG C.
Gained coal tar light component enters the first hydrogenation unit, and the first hydrogenation unit is fixed bed hydrogenation Cracking Unit, according to Secondary filling Hydrobon catalyst and hydrocracking catalyst, admission space ratio are 1:1.The group of the Hydrobon catalyst As NiMoW/Al2O3, the group of hydrocracking catalyst is as NiMoW/Al2O3, wherein the mass content of molecular sieve is 31%. The reaction condition of fixed bed hydrogenation Cracking Unit include: reaction pressure 10.0MPa, hydrofining reaction temperature be 360 DEG C, add hydrogen Cracking reaction temperature is 370 DEG C, and total volume air speed is 1.0h-1, hydrogen to oil volume ratio 1200.
The reaction effluent of first hydrogenation unit is separated and is fractionated, and the yield for obtaining dry gas is 2%, the receipts of liquefied gas Rate is 4.0%, and adding the yield of hydrogen light naphthar is 15%, and adding the yield of hydrogen heavy naphtha is 40%, and the yield of hydrogenated diesel oil is 39%.The property of hydrogen weight naphtha and diesel oil is added to be shown in Table 2.
Hydrogen heavy naphtha is added to be mixed in temperature 70 C with coal tar heavy duty component, coal tar heavy duty component and plus hydrogen scheelite brain The mass ratio of oil after filtering, obtains clarified solution through being sufficiently stirred to obtain clarified solution and insoluble matter after mixing for 5:1.
Gained clarified solution passes through centrifugal separation, obtains fraction I and fraction II.
Gained fraction II, which is contacted into the second hydrogenation unit with hydrogenation catalyst, to be reacted, and the hydrogenation catalyst is sulphur Change iron powder, vulcanizes iron powder and fraction II and mixed with the ratio of mass ratio 1.5/100, and add the CoO of mass fraction 0.5% Solution, reaction condition are as follows: hydrogen partial pressure 7.0MPa, 400 DEG C of reaction temperature, the ratio of hydrogen and reaction raw materials is 800Nm3/ ton, Its reaction effluent obtains adding hydrogen coal tar asphalt after separation and fractionation.
Add hydrogen coal tar asphalt to enter coking tower, in 580 DEG C of coking temperature Coke-oven 6h, obtains the yield of needle coke 45%；The needle coke is calcined under the conditions of 1500 DEG C and obtains ripe coke, thermal expansion coefficient can be obtained by graphitization processing Graphite electrode less than 1 × 10-6/ DEG C.
The property analysis data of 1 full fraction of coal tar of table
Analysis project Data
20 DEG C of density/(g/cm3) 0.9802
Carbon residue/% 3.98
Phenol content/% 13.92
Sulfur content/% 0.28
Nitrogen content/% 0.67
Saturated hydrocarbons/% 29
Aromatic hydrocarbons/% 49
Colloid+asphalitine/% 22
Table 2 plus hydrogen weight naphtha and diesel oil property

Claims (18)

1. a kind of method of coal tar production needle coke and BTX, this method comprises:
(1) full fraction of coal tar raw material after pretreatment, is cut into coal tar light component and coal tar heavy duty component, and light group of coal tar Divide and the cut point of coal tar heavy duty component is 350 DEG C~400 DEG C；
(2) coal tar light component enters the first hydrogenation unit, contacts and is reacted with hydrocracking catalyst, reaction effluent It obtains adding hydrogen light naphthar plus hydrogen heavy naphtha and hydrogenated diesel oil after separation and fractionation；
(3) the resulting coal tar heavy duty component of step (1) adds hydrogen heavy naphtha to be mixed with obtained by step (2), obtains clarified solution And insoluble matter；
(4) clarified solution obtained by step (3) obtains fraction I and fraction II through separation process；
(5) fraction II obtained by step (4) is the coal tar heavy duty component containing low quinoline insolubles, and fraction II enters second plus hydrogen list Member is contacted with hydrogenation catalyst and is reacted under hydrogenation conditions, and reaction effluent obtains after separation and fractionation Add hydrogen coal tar asphalt, the described plus delayed coking of hydrogen coal tar asphalt and calcination process obtain needle coke product；
(6) the fraction I that step (3) obtains is the coal tar light component rich in BTX, and the fraction I obtains BTX after Aromatics Extractive Project Product.
2. the method according to claim 1, wherein in full fraction of coal tar raw material after pretreatment, metal 50 μ g/g of content, 300 μ g/g of water content, 0.01 weight % of content of ashes.
3. the method according to claim 1, wherein the cutting of the coal tar light component and coal tar heavy duty component Point is 360 DEG C~390 DEG C.
4. the method according to claim 1, wherein the first hydrogenation unit is fixed bed hydrogenation Cracking Unit or slurry State bed hydroprocessing Cracking Unit or boiling bed hydrogenation Cracking Unit, preferably fixed bed hydrogenation Cracking Unit.
5. method according to claim 1 or 4, which is characterized in that the reaction condition of the first hydrogenation unit includes: reaction pressure Power is 6~30MPa, and reaction temperature is 320~490 DEG C, and volume space velocity is 0.1~5.0h when liquid-1, hydrogen to oil volume ratio be 200~ 2000。
6. according to the method described in claim 4, it is characterized in that, the reaction condition of fixed bed hydrogenation Cracking Unit includes: anti- Answering pressure is 10~13MPa, and reaction temperature is 350~410 DEG C, and volume space velocity is 0.5~2.0h when liquid-1, hydrogen to oil volume ratio is 800~1500.
7. according to the method described in claim 4, it is characterized in that, loading hydrofinishing in the fixed bed hydrogenation Cracking Unit Catalyst and hydrocracking catalyst, by volume, the filling ratio of Hydrobon catalyst and hydrocracking catalyst are 2:8 ~8:2.
8. the method according to the description of claim 7 is characterized in that containing carrier and load in the Hydrobon catalyst Active metallic element on the carrier, the carrier in aluminium oxide, aluminium oxide-silicon oxide and titanium oxide at least one Kind, the active metallic element is selected from least one of nickel, cobalt, molybdenum and tungsten；Preferably, in Hydrobon catalyst, with The content of the total weight of Hydrobon catalyst, nickel and/or cobalt in terms of oxide is 1~30 weight %, in terms of oxide Molybdenum and/or tungsten content be 5~35 weight %.
9. the method according to the description of claim 7 is characterized in that containing carrier and load in the hydrocracking catalyst Active metallic element on the carrier, the carrier contain molecular sieve and selected from aluminium oxide, aluminium oxide-silicon oxide and oxidations At least one of titanium, the active metallic element are selected from least one of nickel, cobalt, molybdenum and tungsten；The hydrocracking catalyst The heap density of agent is 0.4~1.3g/cm3, hydrocracking catalyst average grain diameter is 0.08~1.2mm, and specific surface area is 100~300m2/g；Preferably, in hydrocracking catalyst, with the total weight of hydrocracking catalyst, molecular sieve content For 10~60 weight %, the content of nickel and/or cobalt in terms of oxide is 1~30%, and the molybdenum and/or tungsten in terms of oxide contain Amount is 5~40 weight %.
10. the method according to claim 1, wherein the first hydrogenation unit reaction effluent is separated and is fractionated After obtain plus hydrogen light naphthar, plus hydrogen heavy naphtha and hydrogenated diesel oil, add hydrogen light naphthar and add cutting between hydrogen heavy naphtha Cutpoint is 60~85 DEG C, and adding the cut point between hydrogen heavy naphtha and hydrogenated diesel oil is 175~190 DEG C；Wherein, add hydrogen pumice brain The yield of oil is 10~20%, and adding the yield of hydrogen heavy naphtha is 15~70%, and hydrogenated diesel oil yield is 5~60%.
11. the method according to claim 1, wherein coal tar heavy duty component and plus hydrogen heavy naphtha in step (3) Mass ratio be 0.1~10, preferred mass ratio be 2~5.
12. the method according to claim 1, wherein coal tar heavy duty component and plus hydrogen heavy naphtha in step (3) Temperature when mixing is 40 DEG C~120 DEG C, preferably 60 DEG C~90 DEG C.
13. the method according to claim 1, wherein separation process described in step (4) be physical partition method, Preferably centrifugal separation.
14. the method according to claim 1, wherein hydrogenation catalyst described in step (5) is iron series catalysis Agent, preferably vulcanization iron powder.
15. according to claim 1 or method described in 14, which is characterized in that the mass ratio 0.001 of hydrogenation catalyst and fraction II ~0.03, preferred mass ratio is 0.005~0.015.
16. according to the method for claim 14, which is characterized in that contain auxiliary agent in the Fe-series catalyst, auxiliary agent is oil The CoO and/or MoO of dissolubility3, the mass ratio of auxiliary agent and fraction II are 0.001~0.02, preferred mass ratio is 0.005~ 0.008。
17. according to the method described in claim 1, it is 350~450 that hydrogenation conditions, which include: reaction temperature, in step (5) DEG C, hydrogen partial pressure is 4.5~13.0MPa, and hydrogen-oil ratio is 300~1500.
18. the method according to claim 1, wherein full fraction of coal tar raw material is middle coalite tar raw material.
CN201810391509.1A 2018-04-27 2018-04-27 Method for producing needle coke and BTX from coal tar Active CN110408433B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201810391509.1A CN110408433B (en) 2018-04-27 2018-04-27 Method for producing needle coke and BTX from coal tar

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201810391509.1A CN110408433B (en) 2018-04-27 2018-04-27 Method for producing needle coke and BTX from coal tar

Publications (2)

Publication Number Publication Date
CN110408433A true CN110408433A (en) 2019-11-05
CN110408433B CN110408433B (en) 2021-03-12

Family

ID=68346242

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201810391509.1A Active CN110408433B (en) 2018-04-27 2018-04-27 Method for producing needle coke and BTX from coal tar

Country Status (1)

Country Link
CN (1) CN110408433B (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114395411A (en) * 2021-12-28 2022-04-26 陕西凯德利能源科技有限公司 System and method for preparing mesophase pitch and oil product based on coal tar hydrogenation

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104250568A (en) * 2013-06-25 2014-12-31 中国石油化工股份有限公司 Treatment process for coal tar-residual oil hydrocracking, catalytic cracking and aromatics extraction
CN204151302U (en) * 2014-08-25 2015-02-11 中国昆仑工程公司 The device of aromatic hydrocarbons is produced in the multistage deep processing of coalite tar
CN106281449A (en) * 2016-10-17 2017-01-04 北京神雾环境能源科技集团股份有限公司 A kind of coal tar produces light Fuel and the method and system of needle coke

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104250568A (en) * 2013-06-25 2014-12-31 中国石油化工股份有限公司 Treatment process for coal tar-residual oil hydrocracking, catalytic cracking and aromatics extraction
CN204151302U (en) * 2014-08-25 2015-02-11 中国昆仑工程公司 The device of aromatic hydrocarbons is produced in the multistage deep processing of coalite tar
CN106281449A (en) * 2016-10-17 2017-01-04 北京神雾环境能源科技集团股份有限公司 A kind of coal tar produces light Fuel and the method and system of needle coke

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114395411A (en) * 2021-12-28 2022-04-26 陕西凯德利能源科技有限公司 System and method for preparing mesophase pitch and oil product based on coal tar hydrogenation

Also Published As

Publication number Publication date
CN110408433B (en) 2021-03-12

Similar Documents

Publication Publication Date Title
CN102465033B (en) Processing method of medium-low temperature coal tar
CN101429456B (en) Delay coking hydrogenation combined process for coal oil
JP7048728B2 (en) Low quality oil reforming method and reforming system
CN101333448B (en) Direct liquefaction process of coal by replacing circling solvent with petroleum or petroleum refining byproduct
CN103289740B (en) Method for preparing clean fuel oil from coal tar
CN102796559B (en) Method and the device of oil fuel are produced in hydrocracking
CN100412168C (en) Coal tar hydrogenation process and catalyst therefor
CN103146411A (en) Process for coal conversion comprising at least one step of liquefaction for the manufacture of aromatics
CN101307256B (en) Coal tar hydrogenating modified method by single-stage method
CN108641749A (en) A kind of hydrogenation combined process producing high-quality fuel by middle coalite tar
CN102453534A (en) Method for producing gasoline and diesel oil through hydrogenation of coal tar
CN104087339A (en) Hydrogenation co-processing method for mixed oil, coal and coal tar
CN103468314B (en) DCL/Direct coal liquefaction circulating solvent and its preparation method and application
CN104004541B (en) A kind of preparation method of coal-based high arene underwater content stock oil
CN103773450A (en) Hydrocracking method for processing inferior raw material
CN106609149B (en) A kind of residual oil and full fraction of coal tar method of hydrotreating
CN102863988B (en) Coal tar combined machining method
CN103468315B (en) DCL/Direct coal liquefaction circulating solvent and its preparation method and application
CN110408433A (en) A kind of method of coal tar production needle coke and BTX
CN103627429B (en) A kind of coal tar faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil
CN110408434A (en) A kind of method of full fraction of coal tar production needle coke and BTX
CN109486519A (en) A kind of method for modifying and system by low-quality oil production high-knock rating gasoline
CN103881750B (en) A kind of coal tar hydrogenation process of maximum using coal tar residue
CN106753553B (en) A kind of device and method of residual oil/coal tar lighting production carbosphere
CN102863987A (en) Hydrocarbon oil pretreatment and catalytic cracking combined technology

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant