CN101302444A - Method for producing oil by hydrocracking of coal-tar pitch - Google Patents
Method for producing oil by hydrocracking of coal-tar pitch Download PDFInfo
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- CN101302444A CN101302444A CNA2008100394243A CN200810039424A CN101302444A CN 101302444 A CN101302444 A CN 101302444A CN A2008100394243 A CNA2008100394243 A CN A2008100394243A CN 200810039424 A CN200810039424 A CN 200810039424A CN 101302444 A CN101302444 A CN 101302444A
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Abstract
The invention relates to a method for producing oil through hydrocracking of coal tar pitch. The method is as follows: firstly, coal tar is taken as solvent, mixed with coal tar pitch, and stirred and dissolved at a temperature of between 100 and 150 DEG C, and filtered filtrate is taken as raw material; secondly, by utilization of the stage continuous processing technique of catalytic hydrocracking of the coal tar pitch through an independent three-stage reaction bed, insoluble solid particles in the coal tar pitch are intercepted and metallic impurities are absorbed in a first-stage fixed bed reactor by adoption of acid mine soil catalyst; the carbon hydrogen ratio of the pitch is reduced through hydrogenation reaction in a second-stage fixed bed reactor by adoption of load nickel-base catalyst, and simultaneously the functions of desulfurization, denitrogeneration, purification and improvement of the pitch are brought into play; catalytic cracking reaction by converting heavy fractions into light fractions and isomerization modification reaction are performed on the hydrorefining pitch in the second stage in a third-stage fixed bed reactor by adoption of modified molecular sieve catalyst; and the coal tar pitch is converted into liquid fuel oil, and the ratio of light oil fractions in the fuel oil is improved. The method is flexible in operation and low in operating cost; and the overall oil yield of the fuel oil can reach over 75 percent. The method is suitable for various coal tar pitches.
Description
Technical field
The present invention relates to a kind of method of producing oil by hydrocracking of coal-tar pitch, relate in particular to a kind of coal-tar pitch hydrogenation and gas reversion oil-producing technique.The technical field that belongs to the coal tar processing and utilization.
Background technology
In the processing and utilization of coal tar, earlier coal tar fractional distillation is become light, heavy several fractions usually, promptly it is divided into several close-cut fractions and tar-bitumens such as light oil, carbolic oil, naphtalene oil, washing oil, carbolineum by distillation.Then from different close-cut fractions through hydrofining or upgrading, be used to produce Chemicals such as phenol, naphthalene, anthracene by separation and Extraction, and the remainder that processing is extracted often mixes oil fuel and uses.As seen the processing of coal tar in the past mainly concentrates on production chemical product aspect.But residual heavy tar pitch accounts for the coal tar total amount up to 50% in the fractionation process, and mainly as producing pitch coke, particularly needle coke, too narrow with respect to the total amount application surface of tar-bitumen, the wider approach that utilizes waits further exploitation to heavy bitumen now; To form the utilization of the heavy bitumen more than 50% be that the processing economy of coal tar is important key and account for coal tar.
At present, petroleum resources face exhaustion, and crude oil price skyrockets, and the increase of fuel demand amount is produced each fuel oils, particularly diesel oil by coal tar and has been subjected to great attention, is in the development phase.CN 20021225737 adopt hydrofinings or modification technology right＜the lightweight coal tar of 350 ℃ of fractions carries out hydrogenation and produces petroleum naphtha and diesel oil.CN 1351130A has proposed the method that a kind of coal tar is produced diesel oil, and it mainly is that lightweight coal tar is carried out hydrofining, is the raising diesel cetane-number, after the hydrofining, again through dearomatization catalyst, to reduce aromaticity content in the product.CN1276059 invention a kind of with low temperature, middle gentle coal-tar heavy oil and from them extraction unit divide residue blending fraction oil behind the chemical industry raw material, comprise that light, heavy coal tar is raw material, hydrofining technology and delay coking process are made up, and production chemical product phenol, naphthalene and oil fuel comprise the method for solvent oil, diesel oil or light-weight fuel oil.In a word, aforesaid method is to adopt light, heavy coal tar production diesel oil, still, adopts tar-bitumen to come each fuel oils of processing as raw material, has not yet to see report.
Summary of the invention
The present invention aims to provide a kind of method of producing oil by hydrocracking of coal-tar pitch.It is not enough to solve the hydrogenation degree to coal-tar pitch that exists with method of the present invention in the coal-tar pitch hydrogenation, can not carry out deep hydrogenation and molecule cracking and make coal-tar pitch be transformed into the problem of oil product.
In order to achieve the above object, the present invention discovers the problem that the refining of petroleum method for hydrogen cracking is easy to rapid deactivation, by slight hydrogenation to coal-tar pitch, be translated into and help as the industrial modified coal tar pitch of carbon raw material, and have and be used to produce high-quality needle coke and properties of carbon, but it is the partial hydrogenation of raw molecule structure, it is complete to keep many cyclic condensations configuration simultaneously, cracking and molecular weight and molecular weight do not take place and makes coal-tar pitch be transformed into the function of oil product.Though CN 1012503B has proposed the heavy bitumen of coal tar is carried out the hydrogenation method of coking production needle coke more after treatment; CN 1011592B discloses the method for hydrotreating of coal-tar pitch, loaded catalyst catalysis contains the slight hydrogenation of the coal-tar pitch of undissolved toluene, make hydrogenated bitumen be fit to produce high-quality needle coke, but as the similar one-part form fixed bed hydrogenation of employing refining of petroleum cracking technology, because coal-tar pitch is rich in the bituminous matter micelle, so effect is relatively poor.Adopt carried catalyst, because reactive behavior depends on the active sites in many passages of carrier substance to a great extent, and this passage is often stopped up by bituminous matter, causes the catalyzer rapid deactivation, lacks practical value to cause continuous catalytic hydrogenation technology.The coal-tar pitch method of hydrotreating of having reported is only to the slight hydrogenation of coal-tar pitch, deep hydrogenation and cracking do not take place and causes the molecular weight and molecular weight of coal-tar pitch component, makes coal-tar pitch be transformed into the oil product effect.The present invention has found a kind of coal-tar pitch purifying treatment and the hydrocracking controllability is good, the method for the high-quality measured coal-tar pitch hydrocracking of fuel oil ratio.This method is totally-enclosed three sections combination serialization productions; In first section reactor based on hold back the insoluble solid particulate, absorption metallic impurity, second section reactor based on hydrogenation reaction reduce pitch hydrocarbon liken to, play the effect of desulfurization removing nitric purifying raising asphalt quality simultaneously, the three-section fixed-bed reactor to hydrofining after pitch carry out catalytic cracking lighting reaction, so that coal-tar pitch is changed into liquid fuel oil.
Concrete processing method and operational condition are as follows:
The first step, with coal tar (this coal tar is the surplus oil after fraction extracts Chemicals) as solvent, mix with coal-tar pitch, blending ratio is a solvent: coal-tar pitch=1: 1 part of quality, then they are heated to 100-150 ℃ and stirring and dissolving, filter at last, remove behind the insoluble solid impurity as raw material for standby.
Second step, the product of raw material and reaction is carried out entering in first section fixed-bed reactor after heat exchange is heated, at temperature 380-420 ℃, pressure 2.2-6.0bar, acid ore deposit scholar's supported nickel catalyst, catalyzed reaction air speed WHSV 0.2-2.0h
-1Carry out preliminary desulfurization removing nitric under the condition, be trapped in the raw material insoluble solid micelle simultaneously and adsorb metallic impurity.Need to specify be that this reactor has insoluble solid micelle (clearance is more than 95%) in the raw material of holding back, decomposes metallic impurity (clearance is more than 98%) in the adsorptive pitch raw material, preliminary desulfurization removing nitric (sulphur/nitrogen＜1.5wt%), and protect the purpose in follow-up second period/the 3rd period catalyzer work-ing life.
The 3rd step, the discharging of first section reactor directly enters in second section fixed-bed reactor through heating, at temperature 402-439 ℃, pressure 3.6-8.0bar, hydrogen/oil ratio 1100/1-1980/1, macroporous aluminium oxide load nickel base catalyzer, catalyzed reaction air speed WHSV 0.36-1.85h
-1Under the condition, make coal-tar pitch generation hydrogenation reaction, its ratio of carbon-hydrogen has big ratio to descend, and reduces to about C/H 9/1 from about C/H 18/1.Employing is played hydrogenation reaction and is reduced pitch ratio of carbon-hydrogen, the further effect of deep desulfuration denitrogenation simultaneously.What need to specify is that catalytic reaction process has the reaction of the coal-tar pitch of making generation deep hydrogenation in this reactor, reduces pitch ratio of carbon-hydrogen, and further deep desulfuration denitrogenation (sulphur/nitrogen＜0.3wt%) significantly.
The 4th step, the discharging of second section reactor directly enters in the three-section fixed-bed reactor through heating, at temperature 406-445 ℃, pressure 1.5-4.7bar, hydrogen/oil ratio 850/1-1600/1, metal oxide modified molecular sieve dual-function catalyst, catalyzed reaction air speed WHSV 0.5-1.95h
-1Under the condition, coal-tar pitch hydrocracking lighting is changed into liquid fuel oil.What need special instruction is that catalytic reaction process has the coal-tar pitch of making generation hydrocracking reaction in this reactor, cause lighting to change into liquid fuel oil, and the ratio of light oil distillate in the raising fuel oil, can reach more than 75% in total oil yield of asphalt stock fuel oil.
In the 5th step, isocrackate is passed to heat through heat exchange and is entered follow-up still kettle behind the raw material of the first step and carry out fractionation, will be lower than to obtain gasoline product after 100 ℃ cut enters condenser condenses; Diesel oil distillate enters diesel oil tank; More heavy oil fraction enters fuel oil tank; The lighter hydrocarbons gas that reclaims from condenser is sent to the industrial furnace internal combustion by the lighter hydrocarbons tracheae.
The present invention compared with prior art, it is as follows that the present invention has significant technique effect:
1. because the present invention has adopted the syllogic fixed-bed reactor that are separated from each other, can independently change raw catalyst respectively, reduce running cost greatly according to the different level of deactivation of each catalyzer; And second section, three-zone hydrocracking catalyst deactivation rate are little, device operation clean energy-saving, for Further Processing of Coal Tar Based Pitch has been opened up a new way, gasoline, diesel oil equal energy source material that present price rises steadily to be done to replenish better, economic benefit will be very considerable.
Since the present invention adopted elder generation with coal tar as solvent, mixes with coal-tar pitch, and 100-150 ℃ of following stirring and dissolving, filtrations rear filtrate is a raw material, therefore be that afterwards catalytic hydrocracking/lighting reaction and isomerization upgrading reacts and become possibility.
3. this technological process is that totally-enclosed serialization operation is produced, and coal-tar pitch is changed into outside the liquid fuel oil, plays the effect of removing metal impurities, desulfurization removing nitric purifying raising fuel qualities simultaneously.Produce by product and can be used as the device fuel energy, the production technique clean environment firendly.
4. the present invention is good to various coal-tar pitch adaptability to raw material, flexible operation, working cost is low, and hydrogenation catalyst cleavage method controllability is good, the qualified fuel oil oil yield is by charging pitch Gao Keda more than 75%, oil quality is good, has realized all kinds of fuel oils of coal-tar pitch hydrocracking direct production.
Specific embodiment
Embodiment 1
The surplus oil that in advance coal tar distillate is extracted after the Chemicals mixes with coal-tar pitch as solvent, solvent: coal-tar pitch=1: 1 part of quality, and be heated to 105 ℃ of following stirring and dissolving, after removing by filter the solid impurity of insolubles then, after reactant feed carried out heat exchange heating, enter in first section fixed-bed reactor, at 380 ℃ of temperature, pressure 2.2bar, catalyzed reaction air speed WHSV 0.2h
-1Carry out preliminary desulfurization removing nitric under the condition, be trapped in the raw material insoluble solid micelle simultaneously and adsorb metallic impurity; Insoluble solid micelle clearance 95.6%, metallic impurity clearance 98.5%, sulphur/nitrogen content 1.3wt%, the discharging of first section reactor directly enters in second section fixed-bed reactor through heating, at 402 ℃ of temperature, pressure 3.6bar, hydrogen/oil ratio 1100/1, catalyzed reaction air speed WHSV 0.36h
-1Under the condition, make coal-tar pitch generation hydrogenation reaction, its ratio of carbon-hydrogen has big ratio to descend, the further effect of deep desulfuration denitrogenation simultaneously, sulphur/nitrogen content 0.23wt%.The discharging of second section reactor directly enters in the three-section fixed-bed reactor through heating, at 406 ℃ of temperature, pressure 1.5bar, and hydrogen/oil ratio 850/1, catalyzed reaction air speed WHSV 0.50h
-1Under the condition, coal-tar pitch hydrocracking lighting is changed into liquid fuel oil, reach 75.5% in total oil yield of asphalt stock fuel oil.
Embodiment 2
The surplus oil part of in advance coal tar distillate being extracted after the Chemicals is mixed with coal-tar pitch as solvent, solvent: coal-tar pitch=1: 1 part of quality, and be heated to 115 ℃ of following stirring and dissolving, after removing by filter the solid impurity of insolubles then, after reactant feed carried out heat exchange heating, enter in first section fixed-bed reactor, at 396 ℃ of temperature, pressure 3.5bar, catalyzed reaction air speed WHSV 0.56h
-1Carry out preliminary desulfurization removing nitric under the condition, be trapped in the raw material insoluble solid micelle simultaneously and adsorb metallic impurity; Insoluble solid micelle clearance 95.9%, metallic impurity clearance 98.7%, sulphur/nitrogen content 1.2wt%, the discharging of first section reactor directly enters in second section fixed-bed reactor through heating, at 413 ℃ of temperature, pressure 4.8bar, hydrogen/oil ratio 1400/1, catalyzed reaction air speed WHSV 0.58h
-1Under the condition, make coal-tar pitch generation hydrogenation reaction, its ratio of carbon-hydrogen has big ratio to descend, the further effect of deep desulfuration denitrogenation simultaneously, sulphur/nitrogen content 0.18wt%.The discharging of second section reactor directly enters in the three-section fixed-bed reactor through heating, at 417 ℃ of temperature, pressure 2.8bar, and hydrogen/oil ratio 1050/1, catalyzed reaction air speed WHSV 0.90h
-1Under the condition, coal-tar pitch hydrocracking lighting is changed into liquid fuel oil, reach 75.8% in total oil yield of asphalt stock fuel oil.
Embodiment 3
The surplus oil part of in advance coal tar distillate being extracted after the Chemicals is mixed with coal-tar pitch as solvent, solvent: coal-tar pitch=1: 1 part of quality, and be heated to 128 ℃ of following stirring and dissolving, after removing by filter the solid impurity of insolubles then, after reactant feed carried out heat exchange heating, enter in first section fixed-bed reactor, at 402 ℃ of temperature, pressure 5.0bar, catalyzed reaction air speed WHSV 1.05h
-1Carry out preliminary desulfurization removing nitric under the condition, be trapped in the raw material insoluble solid micelle simultaneously and adsorb metallic impurity; Insoluble solid micelle clearance 96.0%, metallic impurity clearance 98.6%, sulphur/nitrogen content 1.4wt%, the discharging of first section reactor directly enters in second section fixed-bed reactor through heating, at 425 ℃ of temperature, pressure 6.8bar, hydrogen/oil ratio 1600/1, catalyzed reaction air speed WHSV 1.12h
-1Under the condition, make coal-tar pitch generation hydrogenation reaction, its ratio of carbon-hydrogen has big ratio to descend, the further effect of deep desulfuration denitrogenation simultaneously, sulphur/nitrogen content 0.12wt%.The discharging of second section reactor directly enters in the three-section fixed-bed reactor through heating, at 426 ℃ of temperature, pressure 3.5bar, and hydrogen/oil ratio 1250/1, catalyzed reaction air speed WHSV 1.20h
-1Under the condition, coal-tar pitch hydrocracking lighting is changed into liquid fuel oil, reach 76.5% in total oil yield of asphalt stock fuel oil.
Embodiment 4
The surplus oil part of in advance coal tar distillate being extracted after the Chemicals is mixed with coal-tar pitch as solvent, solvent: coal-tar pitch=1: 1 part of quality, and be heated to 135 ℃ of following stirring and dissolving, after removing by filter the solid impurity of insolubles then, after reactant feed carried out heat exchange heating, enter in first section fixed-bed reactor, at 409 ℃ of temperature, pressure 6.0bar, catalyzed reaction air speed WHSV 1.52h
-1Carry out preliminary desulfurization removing nitric under the condition, be trapped in the raw material insoluble solid micelle simultaneously and adsorb metallic impurity; Insoluble solid micelle clearance 95.6%, metallic impurity clearance 98.2%, sulphur/nitrogen content 1.3wt%, the discharging of first section reactor directly enters in second section fixed-bed reactor through heating, at 436 ℃ of temperature, pressure 7.0bar, hydrogen/oil ratio 1800/1, catalyzed reaction air speed WHSV 1.28h
-1Under the condition, make coal-tar pitch generation hydrogenation reaction, its ratio of carbon-hydrogen has big ratio to descend, the further effect of deep desulfuration denitrogenation simultaneously, sulphur/nitrogen content 0.18wt%.The discharging of second section reactor directly enters in the three-section fixed-bed reactor through heating, at 435 ℃ of temperature, pressure 3.0bar, and hydrogen/oil ratio 1400/1, catalyzed reaction air speed WHSV 1.50h
-1Under the condition, coal-tar pitch hydrocracking lighting is changed into liquid fuel oil, reach 75.7% in total oil yield of asphalt stock fuel oil.
Embodiment 5
The surplus oil part of in advance coal tar distillate being extracted after the Chemicals is mixed with coal-tar pitch as solvent, solvent: coal-tar pitch=1: 1 part of quality, and be heated to 150 ℃ of following stirring and dissolving, after removing by filter the solid impurity of insolubles then, after reactant feed carried out heat exchange heating, enter in first section fixed-bed reactor, at 420 ℃ of temperature, pressure 6.0bar, catalyzed reaction air speed WHSV 2.0h
-1Carry out preliminary desulfurization removing nitric under the condition, be trapped in the raw material insoluble solid micelle simultaneously and adsorb metallic impurity; Insoluble solid micelle clearance 95.1%, metallic impurity clearance 98.1%, sulphur/nitrogen content 1.4wt%, the discharging of first section reactor directly enters in second section fixed-bed reactor through heating, at 439 ℃ of temperature, pressure 8.0bar, hydrogen/oil ratio 1980/1, catalyzed reaction air speed WHSV 1.85h
-1Under the condition, make coal-tar pitch generation hydrogenation reaction, its ratio of carbon-hydrogen has big ratio to descend, the further effect of deep desulfuration denitrogenation simultaneously, sulphur/nitrogen content 0.27wt%.The discharging of second section reactor directly enters in the three-section fixed-bed reactor through heating, at 445 ℃ of temperature, pressure 4.7bar, and hydrogen/oil ratio 1600/1, catalyzed reaction air speed WHSV 1.95h
-1Under the condition, coal-tar pitch hydrocracking lighting is changed into liquid fuel oil, reach 75.3% in total oil yield of asphalt stock fuel oil.
Claims (1)
1, method for producing oil by hydrocracking of coal-tar pitch is characterized in that:
The first step as solvent, is mixed coal tar with coal-tar pitch, blending ratio is a solvent: coal-tar pitch=1: 1, then they are heated to 100-150 ℃ and stirring and dissolving, and filter at last, remove insoluble solid impurity rear filtrate as raw material for standby;
Second step, the product of raw material and reaction is carried out entering in first section fixed-bed reactor after heat exchange is heated, at temperature 380-420 ℃, pressure 2.2-6.0bar, acid ore deposit scholar's supported nickel catalyst, catalyzed reaction air speed WHSV 0.2-2.0h
-1Carry out preliminary desulfurization removing nitric under the condition, make sulphur/nitrogen＜1.5wt%, hold back in the raw material 95% above insoluble solid micelle simultaneously and adsorb 98% above metallic impurity;
The 3rd step, the discharging of first section fixed-bed reactor directly enters in second section fixed-bed reactor through heating, at temperature 402-439 ℃, pressure 3.6-8.0bar, hydrogen/oil ratio 1100/1-1980/1, macroporous aluminium oxide load nickel base catalyzer, catalyzed reaction air speed WHSV 0.36-1.85h
-1Under the condition, make coal-tar pitch send out the degree of depth and give birth to hydrogenation reaction, its ratio of carbon-hydrogen C/H reduces to 9/1 from 18/1, and further deep desulfuration denitrogenation, makes sulphur/nitrogen＜0.3wt%;
The 4th step, the discharging of second section fixed-bed reactor directly enters in the three-section fixed-bed reactor through heating, at temperature 406-445 ℃, pressure 1.5-4.7bar, hydrogen/oil ratio 850/1-1600/1, metal oxide modified molecular sieve dual-function catalyst, catalyzed reaction air speed WHSV 0.5-1.95h
-1Under the condition, coal-tar pitch hydrocracking lighting is changed into liquid fuel oil; And the ratio of light oil distillate in the raising fuel oil, reach more than 75% in total oil yield of asphalt stock fuel oil;
In the 5th step, isocrackate is passed to heat through heat exchange and is entered follow-up still kettle behind the raw material of the first step and carry out fractionation, will be lower than to obtain gasoline product after 100 ℃ cut enters condenser condenses; Diesel oil distillate enters diesel oil tank; More heavy oil fraction enters fuel oil tank; The lighter hydrocarbons gas that reclaims from condenser is sent to the industrial furnace internal combustion by the lighter hydrocarbons tracheae.
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| Application Number | Priority Date | Filing Date | Title |
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| CNA2008100394243A CN101302444A (en) | 2008-06-24 | 2008-06-24 | Method for producing oil by hydrocracking of coal-tar pitch |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102071054A (en) * | 2009-10-30 | 2011-05-25 | 中国石油化工股份有限公司 | Catalytic cracking method |
| CN102212391A (en) * | 2011-05-11 | 2011-10-12 | 同济大学 | Process method for preparing oil by hydrocracking and upgrading coal tar pitch |
| CN102212393A (en) * | 2011-05-11 | 2011-10-12 | 同济大学 | Method for preparing oil through lightening in coal tar pitch hydrogenation and cracking second-order reaction |
| CN102311800A (en) * | 2011-08-29 | 2012-01-11 | 云南昆钢煤焦化有限公司 | Modification method of coal tar pitch needle coke oily by product |
| CN102329637A (en) * | 2011-08-29 | 2012-01-25 | 云南昆钢煤焦化有限公司 | Intensive production method of coal tar pitch needle coke |
| CN103450932A (en) * | 2012-05-31 | 2013-12-18 | 青岛神源生物质能科技有限公司 | Technique of producing fuel oil through normal-pressure catalytic cracking of tar |
| CN104611039A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Poor-quality raw material hydrocracking method |
| WO2015077050A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Process for treatment of pitch from coal tar |
| CN107267204A (en) * | 2017-07-18 | 2017-10-20 | 昆明理工大学 | A kind of heavy oil continuous catalysis cracking device and method |
| CN112111294A (en) * | 2020-09-01 | 2020-12-22 | 中国神华煤制油化工有限公司 | Method and system for preparing oil from coal-based asphalt |
| CN114214076A (en) * | 2021-12-13 | 2022-03-22 | 内蒙古万众炜业科技环保股份公司 | Method for preparing full-particle-size briquette by coal cracking |
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- 2008-06-24 CN CNA2008100394243A patent/CN101302444A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102071054A (en) * | 2009-10-30 | 2011-05-25 | 中国石油化工股份有限公司 | Catalytic cracking method |
| CN102071054B (en) * | 2009-10-30 | 2013-07-31 | 中国石油化工股份有限公司 | Catalytic cracking method |
| CN102212391A (en) * | 2011-05-11 | 2011-10-12 | 同济大学 | Process method for preparing oil by hydrocracking and upgrading coal tar pitch |
| CN102212393A (en) * | 2011-05-11 | 2011-10-12 | 同济大学 | Method for preparing oil through lightening in coal tar pitch hydrogenation and cracking second-order reaction |
| CN102311800A (en) * | 2011-08-29 | 2012-01-11 | 云南昆钢煤焦化有限公司 | Modification method of coal tar pitch needle coke oily by product |
| CN102329637A (en) * | 2011-08-29 | 2012-01-25 | 云南昆钢煤焦化有限公司 | Intensive production method of coal tar pitch needle coke |
| CN102329637B (en) * | 2011-08-29 | 2013-04-24 | 云南昆钢煤焦化有限公司 | Intensive production method of coal tar pitch needle coke |
| CN102311800B (en) * | 2011-08-29 | 2013-04-24 | 云南昆钢煤焦化有限公司 | Modification method of coal tar pitch needle coke oil by-product |
| CN103450932A (en) * | 2012-05-31 | 2013-12-18 | 青岛神源生物质能科技有限公司 | Technique of producing fuel oil through normal-pressure catalytic cracking of tar |
| CN104611039A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Poor-quality raw material hydrocracking method |
| CN104611039B (en) * | 2013-11-05 | 2016-08-17 | 中国石油化工股份有限公司 | Inferior raw material method for hydrogen cracking |
| WO2015077050A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Process for treatment of pitch from coal tar |
| CN107267204A (en) * | 2017-07-18 | 2017-10-20 | 昆明理工大学 | A kind of heavy oil continuous catalysis cracking device and method |
| CN107267204B (en) * | 2017-07-18 | 2019-04-12 | 昆明理工大学 | A kind of heavy oil continuous catalysis cracking device and method |
| CN112111294A (en) * | 2020-09-01 | 2020-12-22 | 中国神华煤制油化工有限公司 | Method and system for preparing oil from coal-based asphalt |
| CN112111294B (en) * | 2020-09-01 | 2022-09-30 | 中国神华煤制油化工有限公司 | Method and system for preparing oil from coal-based asphalt |
| CN114214076A (en) * | 2021-12-13 | 2022-03-22 | 内蒙古万众炜业科技环保股份公司 | Method for preparing full-particle-size briquette by coal cracking |
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