CN103627429A - Combined process for preparing fuel oil by hydro-cracking and hydro-upgrading of coal tar - Google Patents
Combined process for preparing fuel oil by hydro-cracking and hydro-upgrading of coal tar Download PDFInfo
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Abstract
The invention discloses a combined process for preparing fuel oil by hydro-cracking and hydro-upgrading of coal tar, and belongs to the field of coal chemical industries. The coal tar is fractionated through a fractionating tower, then heavy component oil whose boiling point is larger than 360 DEG C and light component oil whose boiling point is lower than 360 DEG C are obtained, the heavy component oil is subjected to a cracking reaction under a hydrogen condition, generated oil formed in the cracking reaction goes back to the fractionating tower, the light component oil whose boiling point is lower than 360 DEG C is subjected to hydro-refining and hydro-cracking systems, so that gasoline and diesel blended components of high quality can be obtained. According to the invention, coke generated is obviously reduced, polymerization and condensation of unsaturated hydrocarbons such as olefin, aromatic hydrocarbons and the like are inhibited, the incidence of coking is reduced, the yield of liquid products obtained through a delayed coking process is improved, working periods of devices are prolonged, and equipment investment is reduced. According to the invention, products of high quality can be produced, and the utilization rate of the coal tar is improved, thereby bringing substantial economic benefits and facilitating environment protection.
Description
Technical field
This patent belongs to coal chemical technology, relates to the combination process that a kind of New type coal tar faces hydrogen cracking and hydro-upgrading made fuel oil.
Background technology
The energy is the important substance basis of national economy sustainable development.The consumption structure of the our times energy still be take petroleum-based energy consumption as main.The standing stock of having verified according to world's crude oil and exploitation situation, expect mid-21st Century, and oil consumption will gradually reduce in energy consumption structure, and natural gas consumption proportion will significantly rise, and consumption of coal proportion remains basically stable.Total Energy situation will be that main being progressively converted into be take Sweet natural gas as main from oil, and then develop into and take coal as main.China is that to belong to petroleum resources in short supply, and natural gas source is not enough, the country that coal is relatively abundant, and coal resources in China workable reserves occupies second place of the world.Coal tar is the staple product of the industry such as coking industry, Coal Chemical Industry and gasification.Along with the development of China's economy, the going from strength to strength of the industries such as iron and steel, chemical industry, coking industry also develops rapidly thereupon, and China has developed into coke the biggest in the world and coal tar is produced country at present.
The further processing means of coal tar is less, utilizes means more single, and price is lower, and product outlet is not smooth yet, is the waste to existing resource, especially in use environment is had to very large impact.The deep processing of coal tar is method of hydrotreating especially, in 20th century five, the sixties, receives much concern and has dropped into substantial contribution and manpower.Then because China finds and recovery of subterranean oil on ground in grand celebration, Xinjiang etc., China's oil has realized self-sufficiency substantially, petroleum products has replaced gelatin liquefaction, gasification to produce oil fuel as main energy sources soon, and the research that coal tar is produced oil fuel has just stopped substantially.Along with the fast development of China's economy, the demand of oil is just increasing, from 1993 Nian Qi China, has become net import of oil state.Oil supply and demand contradiction in short supply has become one of important factor of restriction China Economic development, simultaneously due to the raising of environmental consciousness, the raising of oil Refining Technologies, the raising of people to the understanding of petroleum resources, the comprehensive utilization of coal is paid attention to by knowledgeable people again, and the research of coal tar is revived again.
The heavy constituent that is greater than 360 ℃ in coal tar generally accounts for 50 ~ 60%, and this component is used for producing the raw material of needle coke or modulation pitch at present.If its deep conversion is generated to light-end products, can fully develop the economic worth of coal tar.Patent CN1351130A first carries out fractionation by coal tar, and light ends carries out hydro-upgrading and not further utilization of heavy component, and its weak point is that prepared using degree is lower.Patent CN1147575C discloses a kind of hydrofining treatment process of producing diesel by utilizing coal tar, this invention is also first separated into the full cut of coal tar residual oil and gently slips out oil, gently slip out oil and carry out hydrofining, but equally also do not consider the utilization to residual oil, coal tar utilization ratio is lower.Patent CN1141362C discloses a kind of coal tar hydrogenating process; it is the stable hydrogenation reactor that coal tar and hydrogen enter filling hydrogenation protecting agent and Hydrobon catalyst; the weak point of the method is coal tar necessarily not to be processed before hydrogenation, in hydrogenation process because strong heat release causes temperature runaway and local coking.Patent CN1903994A discloses a kind of method of producing fuel oil by coal tar hydrogenation modifying, the method is mixed in proportion coal tar and thinning oil to carry out hydro-upgrading, though the generation of slow down coking to a certain extent, but active group still exists in coal tar, there is equally may occurring of further polymerization green coke.Patent CN101429456A discloses a kind of delay coking hydrogenation combined process for coal oil, the method combines delay coking of coal tar and hydrogenation technique, obtain liquefied gas, oil fuel and the lubricant base of high-quality, it is low that but weak point is liquid yield, coke yield is high, and coal tar utilization ratio is low.
Summary of the invention
The present invention aim to provide a kind of can be low by being worth, pollute high, easy coking, coal tar that deep processing difficulty is large is converted into gasoline clean, of fine quality and diesel oil or its blend component, improve value-added content of product, the processing method that the coal tar of reduction environmental pollution faces hydrogen cracking and hydro-upgrading made fuel oil.
The combination process process that coal tar of the present invention faces hydrogen cracking and Hydrogenation oil fuel comprises:
A, coal tar raw material is sent into cracking separation column through preheating, what fractionate out is greater than the heavy component oil of 360 ℃ and is less than the light component of 360 ℃, light component oil enters hydrofining operation, after heavy component oil is mixed with hydrogen, be sent to process furnace, after process furnace heats, send into and face hydrogen cleavage column and carry out scission reaction;
B, from facing hydrogen cleavage column, eject the generation oil and the dry gas that come and enter high-pressure separator through heat exchange, isolate dry gas, generate oil through the cooling cracking separation column that enters, heavy component oil returns into process furnace;
C, light component oil mix through hydrofining process furnace and heat with part fresh hydrogen or recycle hydrogen, and enter in hydrofining reactor after mixing with another part fresh hydrogen or recycle hydrogen, under Hydrobon catalyst effect, make hydrogenating materials oil medium sulphide content, nitride and oxide compound respectively with the hydrogen generation hydrogen sulfide that reacts, ammonia and water, through heat exchange, enter hydrofining high-pressure separator, isolating circulating hydrogen returns into reactor, isolated generation oil enters hydrogenation refining fractionation tower, isolates gasoline, diesel oil and tail oil;
D, tail oil mixes through hydrocracking process furnace and heats with part fresh hydrogen or recycle hydrogen, and enter in hydrocracking reactor after mixing with another part fresh hydrogen or recycle hydrogen, under hydrocracking catalyst effect, make long-chain macromolecule hydrocarbon compound in refining tail oil become the micromolecular compound of short chain, saturated and the open loop cracking of the further hydrogenation of aromatic hydroxy compound, make it become micromolecular gasoline and diesel component, through heat exchange, enter hydrocracking high-pressure separator, isolating circulating hydrogen returns into reactor, isolated generation oil enters hydrocracking separation column, isolate gasoline, diesel oil and tail oil.Tail oil enters further cracking in hydrocracking reactor, is finally all converted into gasoline and diesel component;
The condition of e, the wherein cracking described in step a is: preheating temperature is 320 ~ 420 ℃, and process furnace intensification temperature is specially 400 ~ 480 ℃, and facing hydrogen cleavage column reaction pressure is 0.12 ~ 1.0 MPa, hydrogen-oil ratio 0 ~ 60:1.Its main metal (hydrogenation sites) of Hydrobon catalyst described in step c is Mo, and promotor is Ni, Ce and La, and structural promoter is F, and carrier is Al
2o
3, its index is: by mass percentage, and MoO
3be that 15% ~ 30%, NiO is that 2.0% ~ 4.5%, CeO is 2.5% ~ 4.5%, La
2o
3be that 1.5% ~ 3.0%, F is 0.5% ~ 1.5%, pore volume is 0.28 ~ 0.36mL/g, and specific surface area is 100 ~ 300m
2/ g, tap density is 0.65 ~ 0.95g/mL, intensity is greater than 120N/cm, is shaped as trifolium, spherical or bar shaped.Hydrofining condition described in step c is that reaction pressure is specially 8.0 ~ 18.0MPa, and temperature of reaction is 280 ~ 380 ℃, hydrogen-oil ratio 800 ~ 1100:1, volume space velocity 0.2 ~ 0.8h
-1.Its main metal (hydrogenation sites) of hydrocracking catalyst described in steps d is V W, and promotor is Ni, Co and Nd, and structural promoter is P, and carrier is Al
2o
3and beta-molecular sieve, its index is: by mass percentage, and WO
3be that 10% ~ 32%, NiO is that 3.0% ~ 4.3%, CoO is 2.0% ~ 3.8%, Nd
2o
3be that 1.2% ~ 3.5%, P is 2.5% ~ 4.0%, all the other are Al
2o
3and beta-molecular sieve, pore volume is 0.3 ~ 0.36mL/g, specific surface area is 100 ~ 300m
2/ g, tap density is 0.65 ~ 0.95g/mL, intensity is greater than 120N/cm, is shaped as trifolium, spherical or bar shaped.Hydrocracking condition described in steps d is that reaction pressure is 8.0 ~ 18.0MPa, and temperature of reaction is 300 ~ 400 ℃, hydrogen-oil ratio 1000 ~ 1200:1, volume space velocity 0.2 ~ 0.6h
-1.
The present invention take that resource is fully rationally utilized and environmental protection is target, and effectively processing treatment coal tar, solves the coking problem in upgrading process, reduces the coke generation that added value is low and produces more petrol and diesel oil or its blend component, and operation is simple.Key of the present invention is the heavy constituent after coal tar fractional distillation to carry out under the atmosphere of hydrogen preliminary cracking, can obviously reduce coking yield, suppress the incidence that the unsaturated hydrocarbons Type of Collectives such as alkene, aromatic hydrocarbons reduce coking, improve production efficiency of delayed coking liquid product, extend and face hydrogen production device on-stream time, reduce facility investment simultaneously.
Coal tar has complicated character, and its chief component is aromatics, and alkane and olefin(e) centent are less, and aromatic hydrocarbons, heavy metal, colloid, asphalt content are quite high, is also mixed with the compound of a certain amount of nitrogenous, oxygen, sulphur simultaneously.Nitrogenous compound is mainly to have weakly alkaline pyridine, quinoline and its derivates, also contains a certain amount of pyrrole derivative and nitrile compounds simultaneously; Oxygenatedchemicals is mainly to have weakly acidic unit phenol and polyhydric phenols, also contains a certain amount of dibenzofuran, coumarone etc. simultaneously; Sulfocompound is mainly that thiophene, thia indenes, benzo-thiophene etc. contain the compound of thiphene ring and have weakly acidic thiophenol, thionaphthol etc.
Above-mentioned character based on coal tar, the present invention first faces coal tar hydrogen cracking, and scission reaction mainly occurs.Under heating condition, the C-C bond rupture generation scission reaction that in alkane macromole, bond energy is less, alkane and the olefin hydrocarbon molecules of generation small molecules amount.Naphthenic hydrocarbon and aromatic hydrocarbons thermostability are higher, and under comparatively high temps, five-ring, six-ring fracture generate alkene, and benzene starts to occur scission reaction, as the polycyclic aromatic hydrocarbonss such as naphthalene, anthracene also start cracking.But because scission reaction is all carried out facing under hydrogen atmosphere, hydrocarbon cracking trend hydrogenation direction saturated and further fracture is carried out, thereby effectively avoids the condensation between unsaturated hydro carbons.In addition, bituminous matter polycondensation under heat effect is converted into coke, simultaneously by most heavy metal deposition coke.Generate oil and pass into hydrofining tower, sulfide, nitride, oxide compound are reacted and generate hydrogen sulfide, ammonia and water with hydrogen respectively.The light component oil fractionating out further passes into hydrocracking tower, aromatic hydrocarbons and long-chain macromolecule hydro carbons are distinguished saturated and cracking and are generated short chain small molecules hydro carbons and naphthenic hydrocarbon, finally in separation column, fractionate out to meet that processed oil requirement, added value are high, clean, gasoline and the diesel component of high-quality.
The present invention compared with prior art tool has the following advantages: at hydro condition, carry out cracking, slow down or avoided the polycondensation of alkane, arene that coke occurs to produce, the high value kind reducing in coal tar is lost because producing coke; Coal tar enters cracking process furnace, hydrofining process furnace and hydrocracking process furnace together with hydrogen, reduces the incidence of coking, extends to greatest extent the on-stream time of cracking heating furnace device; Can remove more up hill and dale sulphur in coal tar, nitrogen, oxygen heteroatom, improve the stability of hydrogenated products, significantly Improving The Quality of Products; Taken into full account the compositing characteristic of the full cut of coal tar, the in the situation that of assurance device long-term operation, the production lightweight vehicle fuel oil of maximum or its blend component.
Accompanying drawing explanation
Fig. 1 is the combination process schema that coal tar of the present invention faces hydrogen cracking and hydro-upgrading made fuel oil.
Embodiment
Case study on implementation 1 ~ 3
Coupling apparatus schema is done description to the embodiment of this programme, and the present invention is described further.
In conjunction with Fig. 1, coal tar raw material 1 is entered to cracking separation column 2, fractionate out and be greater than the heavy component oil 3 of 360 ℃ and enter cracking process furnace 6 and recycle, fractionate out and be less than the light component oil 4 of 360 ℃ and enter hydrofining operation, the heavy component oil 3 that is preheated to 320 ~ 420 ℃ is mixed and is sent to cracking process furnace 6 with hydrogen 5, be heated to 400 ~ 480 ℃ and enter and face hydrogen cleavage column 7,8 and carry out scission reaction.Control in operation cleavage column reaction pressure 0.28MPa, temperature is controlled at 450 ~ 550 ℃.Hydrogen-oil ratio is controlled: case 1 is 0; Case 2 is 20:1; Case 3 is 40:1.Two are faced hydrogen cleavage column 7,8 was one-period switching running by 18 hours or 24 hours, another cleaning residue 9 during a normal charging.
From cleavage column, eject the gas coming and generate oil 10 and enter separator 11 through heat exchange, isolate dry gas 12, generate oil through the cooling cracking separation column 2 that enters, heavy component oil 3 returns into cleavage column process furnace 6 and enters and face hydrogen cleavage column 7,8 scission reaction occurs again.
Light component oil 4 is mixed into hydrofining process furnace heating 15 as the raw material of hydrogenation and part fresh hydrogen 13 or recycle hydrogen 14, and enter in hydrofining reactor 16 after mixing with another part fresh hydrogen 13 or recycle hydrogen 14, Special hydrogenation catalyst for refining is housed in hydrofining reactor.Controlling in operation reaction stagnation pressure is 8.0 ~ 18.0MPa, and average reaction temperature is 280 ~ 380 ℃, hydrogen-oil ratio 800 ~ 1100:1, volume space velocity 0.2 ~ 0.8h
-1.Its main metal (hydrogenation sites) of Hydrobon catalyst is Mo, and promotor is Ni, Ce and La, and structural promoter is B, and carrier is Al
2o
3, its index is: by mass percentage, and MoO
3be that 15% ~ 30%, NiO is that 2.0% ~ 4.5%, CeO is 2.5% ~ 4.5%, La
2o
3be that 1.5% ~ 3.0%, F is 0.5% ~ 1.5%, all the other are Al
2o
3, pore volume is 0.28 ~ 0.36mL/g, specific surface area is 100 ~ 300m
2/ g, tap density is 0.65 ~ 0.95g/mL, intensity is greater than 120N/cm, is shaped as trifolium, spherical or bar shaped.Like this under the effect of catalyzer hydrogenating materials oil medium sulphide content, nitride and oxide compound respectively with the hydrogen generation hydrogen sulfide that reacts, ammonia and water, through heat exchange, enter hydrofining high-pressure separator 17, isolating circulating hydrogen 14 returns into hydrofining process furnace 15 and hydrofining reactor 16, isolated generation oil enters hydrogenation fractionating tower 18, isolates gasoline 19, diesel oil 20 and tail oil 21; Tail oil 21 mixes with part fresh hydrogen 13 or recycle hydrogen 14 through 22 heating of hydrocracking process furnace, and enter in hydrocracking reactor 23 after mixing with another part fresh hydrogen 13 or recycle hydrogen 14, Special hydrogenation cracking catalyst is housed in hydrocracking reactor.Control in operation hydrofining reaction pressure and be specially 8.0 ~ 18.0MPa, temperature of reaction is 300 ~ 400 ℃, hydrogen-oil ratio 1000 ~ 1200:1, volume space velocity 0.2 ~ 0.6h
-1.Its main metal (hydrogenation sites) of hydrocracking catalyst is W, and promotor is Ni, Co and Nd, and structural promoter is P, and carrier is Al
2o
3and beta-molecular sieve, its index is: by mass percentage, and WO
3be that 10% ~ 32%, NiO is that 3.0% ~ 4.3%, CoO is 2.0% ~ 3.8%, Nd
2o
3be that 1.2% ~ 3.5%, P is 2.5% ~ 4.0%, all the other are Al
2o
3and beta-molecular sieve, pore volume is 0.3 ~ 0.36mL/g, specific surface area is 100 ~ 300m
2/ g, tap density is 0.65 ~ 0.95g/mL, intensity is greater than 120N/cm, is shaped as trifolium, spherical or bar shaped.Under hydrocracking catalyst effect, in refining tail oil, long-chain macromolecule hydrocarbon compound becomes the micromolecular compound of short chain, saturated and the open loop cracking of the further hydrogenation of aromatic hydroxy compound, make it become micromolecular gasoline and diesel oil, through heat exchange, enter hydrocracking high-pressure separator 24, isolating circulating hydrogen 14 returns into hydrocracking process furnace 22 and hydrocracking reactor 23, isolated generation oil enters hydrogenation fractionating tower, isolates gasoline, diesel oil and tail oil.Tail oil enters further cracking in hydrocracking reactor, is finally all converted into gasoline and diesel oil.
Of the present inventionly face hydrogen cracking technology according to the difference of raw material and production object and difference.For example the main character of certain coal tar is in Table 1, and target product is gasoline and diesel oil, and processing condition are in Table 2, and product material forms in Table 3, and the main character of the product of case 2 is in Table 4.
Table 3 product material forms
The main character of table 4 product
Claims (10)
1. a coal tar faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil, it is characterized in that: coal tar fractional distillation is obtained be greater than 360 ℃ a certain temperature section coal tar heavy duty component or without the full cut of coal tar of any processing as charging, under hydro condition, in cleavage column, carry out scission reaction and obtain cracking generation oil, then enter hydro-upgrading system and obtain gasoline and diesel oil.
2. coal tar as claimed in claim 1 faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil, it is characterized in that comprising the steps:
(1) coal tar is sent into after being preheated to 320 ~ 420 ℃ to cracking separation column, the heavy component oil (being greater than 360 ℃) fractionating out and light component oil (being less than 360 ℃), light component oil enters hydrofining operation, heavy component oil is mixed with hydrogen, control hydrogen-oil ratio 0 ~ 200:1, being sent to process furnace is heated to 400 ~ 550 ℃ and enters and face hydrogen cleavage column again, it is that 0.1 ~ 3.0 MPa carries out scission reaction that hydrogen cleavage column reaction pressure is faced in control, alkene under atmosphere of hydrogen, the unsaturated hydro carbons polycondensation such as aromatic hydrocarbons is suppressed and reduce the incidence of coking, the residue producing after scission reaction is discharged continuously at the bottom of facing hydrogen cleavage column, generating oil exports by facing hydrogen cracking tower top with dry gas, through heat exchange, enter high-pressure separator, isolate dry gas, generate oil through the cooling cracking separation column that enters, heavy component oil returns into process furnace,
(2) light component oil mixes through hydrofining process furnace and heats with part fresh hydrogen or recycle hydrogen, and enter in hydrofining reactor after mixing with another part fresh hydrogen or recycle hydrogen, control reaction pressure is 5.0 ~ 20.0MPa, temperature of reaction is 260 ~ 400 ℃, hydrogen-oil ratio 600 ~ 1200:1, volume space velocity 0.2 ~ 1.0h
-1under Hydrobon catalyst effect, make hydrogenating materials oil medium sulphide content, nitride and oxide compound with hydrogen, react and generate hydrogen sulfide, ammonia and water respectively, through heat exchange, enter hydrofining high-pressure separator, isolating circulating hydrogen returns into reactor, isolated generation oil enters hydrogenation fractionating tower, isolates gasoline, diesel oil and tail oil;
(3) tail oil mixes through hydrocracking process furnace and heats with part fresh hydrogen or recycle hydrogen, and enter in hydrocracking reactor after mixing with another part fresh hydrogen or recycle hydrogen, control reaction pressure is 5.0 ~ 20.0MPa, temperature of reaction is 280 ~ 420 ℃, hydrogen-oil ratio 800 ~ 1400:1, volume space velocity 0.2 ~ 1.2h
-1under hydrocracking catalyst effect, in refining tail oil, long-chain macromolecule hydrocarbon compound becomes the micromolecular compound of short chain, saturated and the open loop cracking of the further hydrogenation of aromatic hydroxy compound, make it become micromolecular gasoline and diesel oil, through heat exchange, enter hydrocracking high-pressure separator, isolating circulating hydrogen returns into reactor, isolated generation oil enters hydrogenation fractionating tower, isolate gasoline, diesel oil and circulation tail oil, tail oil enters further cracking in hydrotreater, is finally all converted into gasoline and diesel oil.
3. coal tar as claimed in claim 1 or 2 faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil, it is characterized in that: described coal tar refers to that coal tar, the coal tar of coal tar, the gasification water-gas by-product processed of coking by-product extract phenol or/and the residue cut after naphthalene.
4. coal tar as claimed in claim 2 faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil, in described (1) process, it is characterized in that the described hydrogen cleavage column reaction pressure of facing is 0.12 ~ 1.0 MPa, hydrogen-oil ratio 0 ~ 60:1.
5. coal tar as claimed in claim 2 faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil, in described (1) process, it is characterized in that the described hydrogen cleavage column that faces comprises two, two are faced hydrogen cleavage column cycle blocked operation, during a normal charging, another clears up residue operation.
6. coal tar as claimed in claim 2 faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil, in described (1) process, it is characterized in that described process furnace intensification temperature is specially 400 ~ 480 ℃.
7. coal tar as claimed in claim 2 faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil, in described (2) process, it is characterized in that described control hydrofining reaction pressure is specially 8.0 ~ 18.0MPa, temperature of reaction is 280 ~ 380 ℃, hydrogen-oil ratio 800 ~ 1100:1, volume space velocity 0.2 ~ 0.8h
-1.
8. coal tar as claimed in claim 2 faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil, in described (2) process, it is characterized in that the catalyzer that described unifining process adopts, its main metal (hydrogenation sites) is Mo, promotor is Ni, Ce and La, structural promoter is F, and carrier is Al
2o
3, its index is: by mass percentage, and MoO
3be that 15% ~ 30%, NiO is that 2.0% ~ 4.5%, CeO is 2.5% ~ 4.5%, La
2o
3be that 1.5% ~ 3.0%, F is 0.5% ~ 1.5%, all the other are Al
2o
3, pore volume is 0.28 ~ 0.36mL/g, specific surface area is 100 ~ 300m
2/ g, tap density is 0.65 ~ 0.95g/mL, intensity is greater than 120N/cm, is shaped as trifolium, spherical or bar shaped.
9. coal tar as claimed in claim 2 faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil, in described (3) process, it is characterized in that described control hydrocracking reaction pressure is 8.0 ~ 18.0MPa, temperature of reaction is 300 ~ 400 ℃, hydrogen-oil ratio 1000 ~ 1200:1, volume space velocity 0.2 ~ 0.6h
-1.
10. coal tar as claimed in claim 2 faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil, in described (2) process, it is characterized in that the catalyzer that described hydrocracking process adopts, its main metal (hydrogenation sites) is W, promotor is Ni, Co and Nd, structural promoter is P, and carrier is Al
2o
3and beta-molecular sieve, its index is: by mass percentage, and WO
3be that 10% ~ 32%, NiO is that 3.0% ~ 4.3%, CoO is 2.0% ~ 3.8%, Nd
2o
3be that 1.2% ~ 3.5%, P is 2.5% ~ 4.0%, all the other are Al
2o
3and beta-molecular sieve, pore volume is 0.3 ~ 0.36mL/g, specific surface area is 100 ~ 300m
2/ g, tap density is 0.65 ~ 0.95g/mL, intensity is greater than 120N/cm, is shaped as trifolium, spherical or bar shaped.
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|---|---|---|---|---|
| CN105694971A (en) * | 2016-01-06 | 2016-06-22 | 何巨堂 | High-aromatic hydrogenation and thermal cracking method adopting combined fractionation of raw oil and generated oil |
| CN109652124A (en) * | 2019-02-27 | 2019-04-19 | 伦涛 | No. 180 fuel oil of one kind are hydrocracked production light-weight fuel oil method |
| CN111826187A (en) * | 2020-07-07 | 2020-10-27 | 鞍钢化学科技有限公司 | Novel high-performance asphalt special for carbon material and preparation method thereof |
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| US20050241993A1 (en) * | 2004-04-28 | 2005-11-03 | Headwaters Heavy Oil, Llc | Hydroprocessing method and system for upgrading heavy oil using a colloidal or molecular catalyst |
| CN101240191A (en) * | 2007-02-09 | 2008-08-13 | 中国石油化工股份有限公司 | Method for producing lightweight fuel oil by coal tar heavy fractioning hydrogenation |
| CN101962572A (en) * | 2010-10-29 | 2011-02-02 | 大连理工大学 | Coal tar heavy fraction fluidized-bed hydrocracking method and system thereof |
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| US20050241993A1 (en) * | 2004-04-28 | 2005-11-03 | Headwaters Heavy Oil, Llc | Hydroprocessing method and system for upgrading heavy oil using a colloidal or molecular catalyst |
| CN101240191A (en) * | 2007-02-09 | 2008-08-13 | 中国石油化工股份有限公司 | Method for producing lightweight fuel oil by coal tar heavy fractioning hydrogenation |
| CN101962572A (en) * | 2010-10-29 | 2011-02-02 | 大连理工大学 | Coal tar heavy fraction fluidized-bed hydrocracking method and system thereof |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105694971A (en) * | 2016-01-06 | 2016-06-22 | 何巨堂 | High-aromatic hydrogenation and thermal cracking method adopting combined fractionation of raw oil and generated oil |
| CN109652124A (en) * | 2019-02-27 | 2019-04-19 | 伦涛 | No. 180 fuel oil of one kind are hydrocracked production light-weight fuel oil method |
| CN111826187A (en) * | 2020-07-07 | 2020-10-27 | 鞍钢化学科技有限公司 | Novel high-performance asphalt special for carbon material and preparation method thereof |
| CN111826187B (en) * | 2020-07-07 | 2021-08-24 | 鞍钢化学科技有限公司 | Special high-performance asphalt for carbon material and preparation method thereof |
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Address after: 430223, building 1, innovation base of Chinese workers' science and Technology Park, East Lake Development Zone, Wuhan, Hubei Co-patentee after: SHANGHAI YIZHEN CHEMICAL ENGINEERING Co.,Ltd. Patentee after: Wuhan Kelin Chemical Industry Group Co.,Ltd. Address before: 430223, building 1, innovation base of Chinese workers' science and Technology Park, East Lake Development Zone, Wuhan, Hubei Co-patentee before: SHANGHAI YIZHEN CHEMICAL ENGINEERING Co.,Ltd. Patentee before: WUHAN KELIN FINE CHEMICAL Co.,Ltd. |