CN103695036A - Medium and low temperature coal tar processing method - Google Patents
Medium and low temperature coal tar processing method Download PDFInfo
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Abstract
The invention belongs to the field of the coal chemical industry, and in particular relates to a medium and low temperature coal tar processing method. The method comprises the following steps: removing solid residues from the medium and low temperature coal tar, preprocessing the coal tar to obtain carbolic oil, water and heavy oil; performing phenol extraction on the obtained carbolic oil to obtain a pure phenol product and dephenolized oil; mixing the obtained heavy oil and the obtained dephenolized oil and introducing the mixture in a fluidized bed reactor to perform a hydrogenation reaction, and obtaining modified heavy oil, sulfur-containing and ammonia-containing gas side products; performing hydrorefining and hydrocracking reactions on the modified heavy oil to obtain dry gas, liquefied gas, naphtha, a diesel oil product and a tail oil product. The naphtha and the diesel oil are clean and stable in performance. In addition, a plurality of high value added products are obtained. After hydrotreatment of the fluidized bed, the catalyst service life of the fixed bed reactor is prolonged; furthermore, the heavy component processing problem in the coal tar can be solved. The modified heavy oil after hydrotreatment of the fluidized bed can be subjected to hydrorefining and hydrocracking to improve the oil property.
Description
Technical field
The invention belongs to Coal Chemical Industry technology field, be specifically related to a kind of middle coalite tar processing and treating method.
Background technology
The dry distillation of coal and gasification are the important component parts of Coal Chemical Industry technique, and raw material is main mainly with dross coal or weak caking coal.The dross coal such as brown coal, long-flame coal, bottle coal or weak caking coal all contain abundant organic matter, and when middle low-temperature pyrolysis, half afocal is produced in decapacitation, can also generate coal gas and coal tar, and the mass rate of production of coal tar is generally between 6%～15%; This type of coal gasifies and manufactures coal gas (domestic fuel) or preparing synthetic gas (CO+H
2) while producing other Chemicals, also can produce coal tar, the mass rate of production of coal tar is generally between 4%～12%.
Because middle coalite tar comes from the dry distillation of coal and gasification, be thermally splitting product, so the composition of middle coalite tar is very complicated.The chemical constitution of middle coalite tar is mainly aromatics and alkene, and Determination of Alkane Content is less, also contains a small amount of containing oxygen, nitrogenous, sulfocompound.Oxygenatedchemicals is mainly to have weakly acidic various phenols, and nitrogenous compound is mainly to have weakly alkaline pyridine, quinoline and their derivative, and sulfocompound is mainly thiophene, mercaptan, thiophenol, thioether etc.Deficiency along with China's oil resource, the increase year by year of crude oil import ratio, take middle coalite tar as stock oil, adopts more suitable complete processing to produce clean fuel or the petroleum products suitable with petroleum products, not only there is significant economic benefit, also there is obvious social benefit simultaneously.
CN101538482A provides a kind of middle coalite tar deep processing method.The principal feature of this technique is raw materials pretreatment, dephenolize, and pyrogenic reaction, coking vapour then, diesel oil and wax tailings carry out hydrofining and hydrocracking reaction, obtain gasoline fraction and diesel oil distillate.This technique is by pre-treatment, and pyrogenic reaction and hydrogenation reaction complete.Coal tar unavoidably can generate solid coke in the coking stage, and with petroleum-type coke ratio, accessories of a product value is low for this coke.
CN101633848A provides a kind of middle coalite tar working method, and first this technique carry out fractionation by coal tar, obtains lighting end, carbolic oil, last running and de-tail pitch, carry out phenol removal by carbolic oil, and hydrofining and hydrocracking reaction are carried out in dephenolize oil and lighting end, last running jointly.So, the oil product that enters hydrofining and cracking is only a cut in coal tar, and a large amount of de-tail pitch is well processing not, and the yield of light oil is low.
CN102899087A provides a kind of middle coalite tar deep processing technology method.First middle coalite tar carries out fractionation, obtains lighting end, carbolic oil, and last running and heavy oil, carbolic oil carries out phenol removal, and at the bottom of tower, pyrogenic reaction is carried out in heavy oil and hydrocracking tail oil mixing, and coking product carries out hydrofining and cracking reaction.Different from CA101538482A, the charging of its coking has supplemented hydrocracking tail oil, and coking condition relaxes, and coking yield reduces, but still has coke to generate.
Summary of the invention
For the deficiencies in the prior art, the object of this invention is to provide the full cut complete processing of a kind of middle coalite tar, not only can production high-quality oil product, and coalite tar in farthest utilizing; The present invention has delayed the catalyst life of fixed-bed reactor, has solved the heavy constituent processing problems in coal tar simultaneously; Upgrading heavy oil after boiling bed hydrogenation is passed through to hydrofining and hydrocracking again, improved the character of oil product.
Middle coalite tar processing and treating method of the present invention, comprises the following steps:
(1) middle coalite tar is removed to solid residue, by the solids removal in coal tar, to diameter, be 25 μ m-100 μ m, then carry out pre-treatment;
(2) after step (1) is processed, carry out again fractionation, obtain carbolic oil, water and heavy oil;
(3) carbolic oil step (2) being obtained is carried phenol and is processed, and obtains smart phenolic product and dephenolize oil;
(4) the dephenolize oil obtaining in the heavy oil obtaining in step (2) and step (3) is mixed into ebullated bed reactor and carries out hydrogenation reaction, obtain upgrading heavy oil and sulfur-bearing, contain ammonia gas byproduct;
(5) upgrading heavy oil step (4) being obtained, carries out hydrofining and hydrocracking reaction, obtains dry gas, liquefied gas, petroleum naphtha, diesel product and tail oil product.
Wherein:
The coal tar of low-temperature pyrolysis and/or the coal tar of gasification by-product in the preferred coal of middle coalite tar in step (1).Solid diameter in coal tar is generally 25-1000 μ m, be greater than 100 μ m part solid particulates and be easily adsorbed on hydrogenation catalyst surface, reduce catalyst activity, cause catalyst deactivation, so be first 25 μ m-100 μ m by the solids removal in coal tar to diameter, carry out pre-treatment, pre-treatment is electric desalting and fractionation dehydration again.The Main Function of step (1) is to remove moisture and mechanical impurity.
In step (2), fractionation adopts separation column fractionation, tower top fractionation water outlet, and side line fractionates out carbolic oil, obtains heavy oil at the bottom of tower, and the final boiling point of carbolic oil is not more than 240 ℃.Separation column can be with atmospheric tower or vacuum distillation tower, preferably atmospheric tower.
The phenol of carrying that step (3) is described is processed the soda acid method for extracting that adopts this area routine.The concrete coal tar carbolic oil refining plant that adopts, the carbolic oil that separation column separates enters soda-wash tower, adds alkaline solution, alkaline solution to be preferably the NaOH of concentration 12% or the KOH of concentration 12% in soda-wash tower, and isolated phenates is through steaming stripping oil, sulfuric acid or CO
2after decomposing, obtain crude phenols product, crude phenols product passes through dehydration, de-slag, and phenol rectifying obtains smart phenolic product and dephenolize oil.The smart phenolic product obtaining comprises phenol, ortho-cresol, M-and P-cresols and xylenol etc.
Ebullated bed reactor described in step (4) adds catalyzer while carrying out hydrogenation reaction, because the reaction temperature rising of fixed bed hydrogenation is larger, make easily temperature runaway of reaction itself, handling poor, the present invention adopts ebullated bed reactor hydrogenation, control ebullated bed reactor temperature in well, in reactor, hydrogen oil material is under the stirring of recycle pump, reaction system is constant temperature system, internal activator does not have hot localised points, exothermic heat of reaction is stable and even, and catalyzer overall activity is stable, and catalyst deactivation rate is even.Ebullated bed reactor is lowered the temperature without liquid hydrogen injection simultaneously, greatly reduces discharge capacity and the load of circulating hydrogen compressor.
Ebullated bed reactor has the following advantages:
(1) utilize circulation cup that reactor is divided into two portions, i.e. an annular space part for circulation cup outside, is used for containing catalyst and mixed hydrogen oil product, in circulation cup, is turning oil, and by boosting of recycle pump, the turbulence of raising reactor, makes temperature of reaction even;
(2) circulation cup top design solid-liquid separation riser, the catalyzer of being convenient to be carried is up effectively separated with oil product;
(3) turning oil outlet, turning oil inlet distributor and mixed hydrogen oil-in sparger are arranged at circulation cup bottom;
(4) circulation cup bottom is provided with catalyzer interpolation and draws off pipeline, for catalyzer, adds online and draws off.
The catalyzer when ebullated bed reactor described in step (4) carries out hydrogenation reaction, catalyzer adopts and draws off online and add.Catalyzer adds and draws off is at catalyzer, to add/draw off between tank and reactor to carry out.When adding catalyzer, set up catalyzer add/draw off tank with pressure difference between reactor at 0-2.0MPa, utilize oil product to carry with pressure difference catalyzer added in reactor.When catalyzer draws off, set up catalyzer add/draw off tank with pressure difference between reactor at-2.0-0MPa, utilize oil product to carry, with pressure difference, the catalyzer in reactor is discharged to catalyzer and add/draw off tank.Catalyzer draws off and is added to and intermittently carries out, and draws off and the assist medium that adds is hydrogen, oil product and nitrogen.What boiling bed hydrogenation technique was processed is full cut coal tar, at high temperature can generating portion Absorption of Coke be attached to catalyst surface.By boiling bed hydrogenation technique, can draw off online part decaying catalyst, add the average activity that part catalyzer fresh or that regenerated improves the catalyzer in reactor simultaneously.
The active ingredient of the catalyzer of boiling bed hydrogenation is preferably Ni, Co or Mo metal, but because it flows in reactor, different with typical catalyst, require hardness more than 15N/mm2, prevent that catalyzer from forming powder.
The reaction conditions of the hydrogenation reaction described in step (4) is: 280 ℃～500 ℃ of temperature of reaction, reaction pressure 10MPa～20MPa; Volume space velocity 0.1～2h when hydrogen to oil volume ratio 500:1～2000:1 and liquid
-1; Be preferably 300 ℃～480 ℃ of temperature of reaction, reaction pressure 12MPa～18MPa, volume space velocity 0.2～1.5h when hydrogen to oil volume ratio 500:1～1500:1 and liquid
-1.
Hydrofining and hydrocracking in step (5) adopt technological process well known to those skilled in the art, hydrofining effluent generally need carry out separating treatment, the water that the impurity removing in hydrofining reaction process is particularly produced is separated, and then carries out hydrocracking reaction.Avoid hydrocracking to have a negative impact, a kind of typical method is to adopt two-stage hydrocracking technique.Hydrofining reaction product, before entering hydrocracking reactor, first enters separation column.Hydrofining and hydrocracking reaction are specially: hydrofining reaction product is before entering hydrocracking reactor, be introduced into separation column, hydrotreated product is obtained to naphtha fraction by fractionation, diesel oil distillate, dry gas, liquefied gas and tail oil cut, the direct carrying device of naphtha fraction and diesel oil distillate, tail oil cut mixes and carries out hydrocracking reaction with the unconverted oil producing after hydrocracking reaction, isocrackate is obtained to naphtha fraction by fractionation, diesel oil distillate, dry gas, liquefied gas, unconverted oil and tail oil, the unconverted oil that hydrocracking produces is mixed and is carried out hydrocracking reaction again with the tail oil cut of hydrofining generation, for guaranteeing the activity of catalyzer, outer the getting rid of of tail oil part that hydrocracking produces, this part tail oil can be used as oil fuel and sells.
Hydrofining reaction condition in step (5) is: volume space velocity 0.1～2h when 200～450 ℃ of temperature of reaction, pressure 10.0～18.0MPa, hydrogen to oil volume ratio 500:1～2000:1 and liquid
-1; Preferred reaction conditions is as follows: volume space velocity 0.2～1.5h when 220～430 ℃ of temperature of reaction, pressure 10.0～16.0MPa, hydrogen to oil volume ratio 800:1～1500:1 and liquid
-1.
Hydrocracking reaction condition in step (5) is: volume space velocity 0.1～2h when 360～450 ℃ of temperature of reaction, pressure 10.0～18.0MPa, hydrogen to oil volume ratio 500:1～2000:1 and liquid
-1; Preferred reaction conditions is as follows: volume space velocity 0.2～1.5h when 380～430 ℃ of temperature of reaction, pressure 10.0～16.0MPa, hydrogen to oil volume ratio 800:1～1500:1 and liquid
-1.
The hydrofining and the hydrocracking reaction that in the hydrogenation reaction of carrying out in ebullated bed reactor in step (4), step (5), carry out, the hydrogen of hydrogenation used can derive from one or more in dry distillation of coal coal gas, gasification coal gas, natural gas hydrogen preparation, oil refinery dry gas hydrogen manufacturing and hydrogen from methyl alcohol, the concentrate of low-concentration hydrogen can adopt this area ordinary method, as pressure-changed adsorption concentrating method etc.
Compared with prior art, the present invention has the following advantages:
(1) the present invention adopts full cut reconstructed coal tar, there is no coke and de-tail asphaltic products. in processed products, and the yield of light oil is high.
(2) boiling bed process solved fixed-bed reactor working pressure fall increase too fast, the problem such as catalyst operation is short, the catalyzer by ebullated bed adds online and draws off technique, has solved the fast and device short problem of operational cycle of catalyst deactivation.
(3) the present invention obtains naphtha fraction and diesel oil distillate clean, stable performance.In addition, utilize the singularity of coal tar component also to produce the high value added products such as phenol, ortho-cresol, M-and P-cresols, xylenol, liquefied gas.Really realize effective utilization of middle coalite tar, more greatly improved the rate of utilization of coal tar.
(4) phenols has deep-etching effect to equipment, and has high added value, therefore before to coal tar deep processing, first isolates phenol products, has not only increased economic benefit, has extended the work-ing life of coal tar deep processing appliance arrangement simultaneously.
(5) because coal tar aromaticity content is large, heavy constituent is many, and after adopting boiling bed hydrogenation to process, upgrading heavy oil can all enter fixed-bed reactor, has delayed the catalyst life of fixed-bed reactor, has solved the heavy constituent processing problems in coal tar simultaneously.The service temperature of ebullated bed reactor is easily controlled, and catalyzer adopts and adds online and draw off, and has greatly improved the operational cycle of device.The operational cycle of general fixed bed hydrogenation is 1-3, and ebullating bed reactor is not limited.Ebullated bed reactor has been avoided the hot localised points of catalyzer, has also reduced the production rate of coke.
(6) upgrading heavy oil after boiling bed hydrogenation is passed through to hydrofining and hydrocracking again, can greatly improve the character of oil product, maximum ground produces high-quality petrol and diesel oil cut, in oil supply day, be becoming tight, in the situation that light-end products demand goes up, provide the source of supply of new light-end products.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of the full cut complete processing of coalite tar in the present invention.
Embodiment
Below in conjunction with embodiment, the present invention will be further described.
Embodiment 1
(1) the low-temperature pyrolysis coal tar of Shenmu County's brown coal, character, in Table 1, is sent pretreatment unit to and is removed solid impurity, and electric desalting and fractionation dehydration, be 50um by the solids removal in coal tar to diameter;
(2) after step (1) is processed, enter again atmospheric fractional tower and carry out fractionation, fractionation water outlet, carbolic oil (side line) and heavy oil;
(3) carbolic oil step (2) being obtained is carried phenol and is processed, and enters carbolic oil extraction plant and isolates smart phenolic product and dephenolize oil;
(4) the dephenolize oil obtaining in the heavy oil obtaining in step (2) and step (3) is mixed into ebullated bed reactor and carries out hydrogenation reaction, obtain upgrading heavy oil and sulfur-bearing, contain ammonia gas byproduct; 360 ℃ of temperature of reaction, reaction pressure 12MPa, volume space velocity 1.0h when hydrogen to oil volume ratio 500:1 and liquid
-1;
(5) upgrading heavy oil step (4) being obtained, carry out hydrofining and hydrocracking reaction, hydrofining reaction product is before entering hydrocracking reactor, be introduced into separation column, hydrotreated product is obtained to naphtha fraction by fractionation, diesel oil distillate, dry gas, liquefied gas and tail oil cut, the direct carrying device of naphtha fraction and diesel oil distillate, tail oil cut mixes and carries out hydrocracking reaction with the unconverted oil producing after hydrocracking reaction, isocrackate is obtained to naphtha fraction by fractionation, diesel oil distillate, dry gas, liquefied gas, unconverted oil and tail oil, tail oil part is outer gets rid of.Volume space velocity 0.5h when hydrorefined temperature of reaction is 320 ℃, pressure 12.0MPa, hydrogen to oil volume ratio 1000:1 and liquid
-1; Volume space velocity 0.4h when 390 ℃ of the temperature of reaction of hydrocracking, pressure 12.0MPa, hydrogen to oil volume ratio 800:1 and liquid
-1.
Hydrobon catalyst is with alumina supporter, and molybdenum oxide weight content is 15%, and Tungsten oxide 99.999 weight content is 12%, and nickel oxide weight content is 5%, and specific surface area is 185m
2/ g, pore volume is 0.35ml/g.It is cracking component that hydrocracking catalyst be take Y zeolite (silica/alumina molecular ratio is 12) and amorphous aluminum silicide (silica weight content is 27%), Y zeolite weight content is 15%, amorphous aluminum silicide weight content is 35%, Tungsten oxide 99.999 weight content is 28%, nickel oxide weight content is 8%, surplus is aluminum oxide, and specific surface area is 270m
2/ g, pore volume is 0.42ml/g.
Embodiment 2
(1) the middle low-temperature pyrolysis coal tar of Shenmu County's brown coal, character, in Table 2, is sent pretreatment unit to and is removed solid impurity, and electric desalting and fractionation dehydration, be 40um by the solids removal in coal tar to diameter;
(2) after step (1) is processed, enter again atmospheric fractional tower and carry out fractionation, fractionation water outlet, carbolic oil (side line) and heavy oil;
(3) carbolic oil step (2) being obtained is carried phenol and is processed, and enters carbolic oil extraction plant and isolates smart phenolic product and dephenolize oil;
(4) the dephenolize oil obtaining in the heavy oil obtaining in step (2) and step (3) is mixed into ebullated bed reactor and carries out hydrogenation reaction, obtain upgrading heavy oil and sulfur-bearing, contain ammonia gas byproduct; 380 ℃ of temperature of reaction, reaction pressure 16MPa, volume space velocity 1.0h when hydrogen to oil volume ratio 500:1 and liquid
-1;
(5) upgrading heavy oil step (4) being obtained, carry out hydrofining and hydrocracking reaction, hydrofining reaction product is before entering hydrocracking reactor, be introduced into separation column, hydrotreated product is obtained to naphtha fraction by fractionation, diesel oil distillate, dry gas, liquefied gas and tail oil cut, the direct carrying device of naphtha fraction and diesel oil distillate, tail oil cut mixes and carries out hydrocracking reaction with the unconverted oil producing after hydrocracking reaction, isocrackate is obtained to naphtha fraction by fractionation, diesel oil distillate, dry gas, liquefied gas, unconverted oil and tail oil, tail oil part is outer gets rid of.Hydrorefined temperature of reaction is 300 ℃, pressure 16.0MP
a, volume space velocity 0.4h when hydrogen to oil volume ratio 1000:1 and liquid
-1; 400 ℃ of the temperature of reaction of hydrocracking, pressure 16.0MP
a, volume space velocity-0.3h when hydrogen to oil volume ratio 1200:1 and liquid
-1.
Hydrobon catalyst is with alumina supporter, and molybdenum oxide weight content is 15%, and Tungsten oxide 99.999 weight content is 12%, and nickel oxide weight content is 5%, and specific surface area is 185m
2/ g, pore volume is 0.35ml/g.It is cracking component that hydrocracking catalyst be take Y zeolite (silica/alumina molecular ratio is 12) and amorphous aluminum silicide (silica weight content is 27%), Y zeolite weight content is 15%, amorphous aluminum silicide weight content is 35%, Tungsten oxide 99.999 weight content is 28%, nickel oxide weight content is 8%, surplus is aluminum oxide, and specific surface area is 270m
2/ g, pore volume is 0.42ml/g.
The main character of the low-temperature pyrolysis coal tar of table 1 Shenmu County brown coal
| Raw material | Coalite tar |
| Density (20 ℃), g/cm 3 | 1.02 |
| Boiling range, ℃ | ? |
| IBP/10% | 102.8/188.8 |
| 30%/50％ | 245.2/338.0 |
| 70％/90％ | 395.0/445.2 |
| 95％/FBP | 484.0/-- |
| S，wt％ | 0.39 |
| N，μg·g －1 | 7986 |
The main character of the middle low-temperature pyrolysis coal tar of table 2 Shenmu County brown coal
| Raw material | Middle coalite tar |
| Density (20 ℃), g/cm 3 | 1.06 |
| Boiling range, ℃ | ? |
| IBP/10% | 160/240 |
| 30%/50％ | 310/362 |
| 70％/80％ | 418/460 |
| FBP | --- |
| S，wt％ | 0.16 |
| N，μg·g －1 | 9200 |
Table 3-5 is the main character of the product that obtains of the present invention.
The mixing petroleum naphtha character that table 3 hydrofining of the present invention and hydrocracking obtain
| Density (20 ℃), gcm -3 | 0.758 |
| Boiling range, ℃ | ? |
| IBP/10% | 87/105 |
| 30%/50% | 113/124 |
| 70%/90% | 133/153 |
| EBP | 168 |
| S，μg·g -1 | <0.5 |
| N，μg·g -1 | <0.5 |
| Virtue is dived, % | 75 |
The Medium diesel oil character that table 4 hydrofining diesel oil of the present invention and hydrocracking obtain
| Density (20 ℃), gcm -3 | 0.869 |
| Boiling range, ℃ | ? |
| IBP/10% | 163/210 |
| 30%/50% | 222/236 |
| 70%/90% | 254/287 |
| 95%/EBP | 305/342 |
| Viscosity (20 ℃), mm 2·s -1 | ? |
| Acidity, mgKOH (100mL) -1 | 1.57 |
| Flash-point, ℃ | 55 |
| Condensation point, ℃ | <-50 |
| Cold filter clogging temperature, ℃ | <-35 |
| Cetane value | 42 |
| S，μg·g -1 | <10 |
| N，μg·g -1 | <10 |
The physical properties of several main lower boiling phenol that table 5 the present invention obtains
Table 6 is the standard index of phenol and technical xylenol; Table 6 is the standard index of cresols.
The standard index of table 6 phenol and technical xylenol
The standard index of table 7 cresols
Claims (9)
1. a coalite tar processing and treating method in, is characterized in that: comprise the following steps:
(1) middle coalite tar being removed to solid residue, is 25um-100um by the solids removal in coal tar to diameter, then carries out pre-treatment;
(2) after step (1) is processed, carry out again fractionation, obtain carbolic oil, water and heavy oil;
(3) carbolic oil step (2) being obtained is carried phenol and is processed, and obtains smart phenolic product and dephenolize oil;
(4) the dephenolize oil obtaining in the heavy oil obtaining in step (2) and step (3) is mixed into ebullated bed reactor and carries out hydrogenation reaction, obtain upgrading heavy oil and sulfur-bearing, contain ammonia gas byproduct;
(5) upgrading heavy oil step (4) being obtained, carries out hydrofining and hydrocracking reaction, obtains dry gas, liquefied gas, petroleum naphtha, diesel product and tail oil product.
2. middle coalite tar processing and treating method according to claim 1, is characterized in that: in step (1), pre-treatment is electric desalting and fractionation dehydration.
3. middle coalite tar processing and treating method according to claim 1, is characterized in that: in step (2), fractionation adopts separation column fractionation, tower top fractionation water outlet, and side line fractionates out carbolic oil, obtains heavy oil at the bottom of tower, and the final boiling point of carbolic oil is not more than 240 ℃.
4. according to the middle coalite tar processing and treating method described in claim 1 or 3, it is characterized in that: step (3) is described carries phenol and be treated to the carbolic oil that separation column separates and enter soda-wash tower, in soda-wash tower, add alkaline solution, isolated phenates is through steaming stripping oil, sulfuric acid or CO
2after decomposing, obtain crude phenols product, crude phenols product passes through dehydration, de-slag, and phenol rectifying obtains smart phenolic product and dephenolize oil.
5. middle coalite tar processing and treating method according to claim 1, is characterized in that: the ebullated bed reactor described in step (4) adds catalyzer while carrying out hydrogenation reaction, and catalyzer adopts and draws off online and add.
According to claim 1 or 5 in coalite tar processing and treating method, it is characterized in that: the reaction conditions of the hydrogenation reaction described in step (4) is: 280 ℃～500 ℃ of temperature of reaction, reaction pressure 10MPa～20MPa, volume space velocity 0.1～2h when hydrogen to oil volume ratio 500:1～2000:1 and liquid
-1.
7. middle coalite tar processing and treating method according to claim 1, it is characterized in that: the hydrofining described in step (5) and hydrocracking reaction are: hydrofining reaction product is before entering hydrocracking reactor, be introduced into separation column, hydrotreated product is obtained to naphtha fraction by fractionation, diesel oil distillate, dry gas, liquefied gas and tail oil cut, the direct carrying device of naphtha fraction and diesel oil distillate, tail oil cut mixes and carries out hydrocracking reaction with the unconverted oil producing after hydrocracking reaction, isocrackate is obtained to naphtha fraction by fractionation, diesel oil distillate, dry gas, liquefied gas, unconverted oil and tail oil, tail oil part is outer gets rid of.
8. middle coalite tar processing and treating method according to claim 1, is characterized in that: in step (5), hydrofining reaction condition is: volume space velocity 0.1～2h when 200～450 ℃ of temperature of reaction, pressure 10.0～18.0MPa, hydrogen to oil volume ratio 500:1～2000:1 and liquid
-1.
9. according to the middle coalite tar processing and treating method described in claim 1,7 or 8, it is characterized in that: hydrocracking reaction condition is in step (5): volume space velocity 0.1～2h when 360～450 ℃ of temperature of reaction, pressure 10.0～18.0MPa, hydrogen to oil volume ratio 500:1～2000:1 and liquid
-1.
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| CN103965078A (en) * | 2014-05-05 | 2014-08-06 | 大连理工大学 | Method for preparing benzonitrile and clean fuel from dephenolized carbolic oil |
| CN105316018A (en) * | 2014-08-02 | 2016-02-10 | 长江(扬中)电脱盐设备有限公司 | Pretreatment method for deep processing of coal tar |
| CN105694967A (en) * | 2014-11-25 | 2016-06-22 | 神华集团有限责任公司 | Processing method for coal tar and high-octane-number gasoline prepared by using same |
| CN106047406A (en) * | 2016-07-13 | 2016-10-26 | 北京华福工程有限公司 | Coal tar hydrogenation reaction device and method for rapidly recycling light hydrocarbons |
| CN106701171A (en) * | 2015-11-16 | 2017-05-24 | 神华集团有限责任公司 | Machining method of phenol-containing oil in coal tar and machining method of coal tar |
| CN108300511A (en) * | 2018-03-13 | 2018-07-20 | 中国五环工程有限公司 | Middle coalite tar two-stage hydrogenation treatment process and its system |
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| CN113174273A (en) * | 2021-04-09 | 2021-07-27 | 煤炭科学技术研究院有限公司 | Coal tar purification method |
| CN114437824A (en) * | 2020-10-30 | 2022-05-06 | 中国科学院宁波材料技术与工程研究所 | Method for producing clean fuel from coal tar whole fraction |
| CN114433118A (en) * | 2020-10-30 | 2022-05-06 | 中国科学院宁波材料技术与工程研究所 | Fluidized bed hydrogenation catalyst and processing method of coal tar whole fraction |
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| CN108300511B (en) * | 2018-03-13 | 2023-12-15 | 中国五环工程有限公司 | Two-stage hydrotreating process and system for medium-low temperature coal tar |
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| CN114437824B (en) * | 2020-10-30 | 2023-01-17 | 中国科学院宁波材料技术与工程研究所 | Method for producing clean fuel from coal tar whole fraction |
| CN114433118B (en) * | 2020-10-30 | 2023-06-02 | 中国科学院宁波材料技术与工程研究所 | Ebullated bed hydrogenation catalyst and method for processing coal tar full fraction |
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