CN103627429B - A kind of coal tar faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil - Google Patents
A kind of coal tar faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil Download PDFInfo
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Abstract
Coal tar faces a combination process for hydrogen cracking and hydro-upgrading made fuel oil, belongs to coal chemical technology.This technique by coal tar through separation column fractionation, obtain the heavy component oil higher than 360 DEG C and the light component oil lower than 360 DEG C, heavy component oil carries out scission reaction under hydro condition, the generation oil of cracking returns into separation column, enter hydrofining and hydrocracking system lower than the light component oil of 360 DEG C, gasoline and the diesel oil blending component of high-quality can be obtained.Present invention process obviously can reduce coke and generate, and suppresses the unsaturated hydrocarbons Type of Collective such as alkene, aromatic hydrocarbons and condensation, reduces the incidence of coking, and improve production efficiency of delayed coking liquid product, extension fixture on-stream time, reduces facility investment simultaneously.The present invention can yield products of quality, and improves the utilization ratio of coal tar, not only has significant economic benefit, also help protection of the environment simultaneously.
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 is still based on petroleum-based energy consumption.The standing stock 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 master is progressively converted into based on Sweet natural gas from oil, and then develop into based on coal.China is that to belong to petroleum resources in short supply, and natural gas source is not enough, and the country of coal relative abundance, 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, going from strength to strength of the industry such as iron and steel, chemical industry, coking industry also develops rapidly thereupon, and current China has developed into coke the biggest in the world and coal tar produces country.
The further processing means of coal tar is less, utilize means more single, and price is lower, and product outlet is not smooth yet, is the waste to existing resource, especially in use has very large impact to environment.The deep processing especially method of hydrotreating of coal tar, receives much concern in 20th century five, the sixties and has dropped into substantial contribution and manpower.Then because China finds and recovery of subterranean oil on the ground such as grand celebration, Xinjiang, China's oil achieves self-sufficiency substantially, petroleum products instead of gelatin liquefaction soon as main energy sources, oil fuel is produced in gasification, and the research that coal tar produces oil fuel just stopped substantially.Along with the fast development of China's economy, the demand of oil is just increasing, has become net import of oil state from 1993 Nian Qi China.Oil supply and demand contradiction in short supply has become one of important factor of restriction China Economic development, simultaneously because the raising of the raising of environmental consciousness, oil Refining Technologies, people are to the raising of 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 being greater than 360 DEG C in coal tar generally accounts for 50 ~ 60%, and this component is used for the raw material producing needle coke or modulation pitch at present.If its deep conversion is generated light-end products, the economic worth of coal tar fully can be developed.Coal tar is first carried out fractionation by patent CN1351130A, and light ends carries out hydro-upgrading and heavy component does not utilize further, 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, full fraction of coal tar is also first separated into residual oil and gently slips out oil by this invention, 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; that coal tar and hydrogen enter the stable hydrogenation reactor loading hydrogenation protecting agent and Hydrobon catalyst; coal tar is not necessarily processed before the weak point of the method is hydrogenation, because very exothermic causes temperature runaway and local coking in hydrogenation process.Patent CN1903994A discloses a kind of method of producing fuel oil by coal tar hydrogenation modifying, coal tar and thinning oil are mixed in proportion by the method carries out hydro-upgrading, though the generation of slow down coking to a certain extent, but active group still exists in coal tar, have equally and be polymerized may occurring of green coke further.Patent CN101429456A discloses a kind of delay coking hydrogenation combined process for coal oil, delay coking of coal tar and hydrogenation technique combine by the method, obtain the liquefied gas of high-quality, oil fuel and lubricant base, but weak point is that liquid yield is low, 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 by be worth low, 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 coal tar reducing environmental pollution faces the processing method of 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 DEG C and is less than the light component of 360 DEG C, light component oil enters hydrofining operation, be sent to process furnace after mix with hydrogen by heavy component oil, after process furnace heats, feeding is faced hydrogen cleavage column and is carried out scission reaction;
B, from face hydrogen cleavage column eject come generation oil and dry gas enter high-pressure separator through heat exchange, isolate dry gas, generate oil then through cooling enter cracking separation column, heavy component oil returns into process furnace;
C, light component oily mixing with part fresh hydrogen or recycle hydrogen heats through hydrofining process furnace, and enter in hydrofining reactor after mixing with another part fresh hydrogen or recycle hydrogen, under Hydrobon catalyst effect, make Hydrogenation raw oil medium sulphide content, nitride and oxide compound react generation hydrogen sulfide with hydrogen respectively, ammonia and water, hydrofining high-pressure separator is entered through heat exchange, 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 with part fresh hydrogen or recycle hydrogen and heats through hydrocracking process furnace, 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, the further hydrotreated lube base oil of aromatic hydroxy compound open loop cracking, it is made to become micromolecular gasoline and diesel component, hydrocracking high-pressure separator is entered through heat exchange, 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, cracking wherein described in step a is: preheating temperature is 320 ~ 420 DEG C, and process furnace warming temperature is specially 400 ~ 480 DEG C, and facing hydrogen cleavage column reaction pressure is 0.12 ~ 1.0MPa, 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, MoO
3be 15% ~ 30%, NiO be 2.0% ~ 4.5%, CeO be 2.5% ~ 4.5%, La
2o
3be 1.5% ~ 3.0%, F be 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, and intensity is greater than 120N/cm, and shape is trifolium, spherical or bar shaped.Hydrofinishing conditions described in step c is that reaction pressure is specially 8.0 ~ 18.0MPa, and temperature of reaction is 280 ~ 380 DEG C, 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 VW, 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, WO
3be 10% ~ 32%, NiO be 3.0% ~ 4.3%, CoO be 2.0% ~ 3.8%, Nd
2o
3be 1.2% ~ 3.5%, P be 2.5% ~ 4.0%, all the other are Al
2o
3and beta-molecular sieve, pore volume is 0.3 ~ 0.36mL/g, and specific surface area is 100 ~ 300m
2/ g, tap density is 0.65 ~ 0.95g/mL, and intensity is greater than 120N/cm, and shape is trifolium, spherical or bar shaped.Hydrocracking condition described in steps d is reaction pressure is 8.0 ~ 18.0MPa, and temperature of reaction is 300 ~ 400 DEG C, hydrogen-oil ratio 1000 ~ 1200:1, volume space velocity 0.2 ~ 0.6h
-1.
The present invention with the abundant Appropriate application of resource and environmental protection for target, can effective processing treatment coal tar, solve the coking problem in upgrading processes, reduce the low coke of added value and produce and produce more petrol and diesel oil or its blend component, operation is simple.The present invention's key is that the heavy constituent after by coal tar fractional distillation carries out preliminary cracking under the atmosphere of hydrogen, obviously can reduce coking yield, the unsaturated hydrocarbons such as alkene, aromatic hydrocarbons Type of Collective is suppressed to reduce the incidence of 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 it mainly forms is aromatics, alkane and olefin(e) centent less, aromatic hydrocarbons, heavy metal, colloid, asphalt content are quite high, are also mixed with the compound of a certain amount of nitrogenous, oxygen, sulphur simultaneously.Nitrogenous compound mainly has weakly alkaline pyridine, quinoline and its derivates, simultaneously also containing a certain amount of pyrrole derivative and nitrile compounds; Oxygenatedchemicals mainly has weakly acidic unit phenol and polyhydric phenols, simultaneously also containing a certain amount of dibenzofuran, coumarone etc.; Sulfocompound mainly thiophene, thia indenes, benzo-thiophene etc. contains the compound of thiphene ring and has weakly acidic thiophenol, thionaphthol etc.
Based on the above-mentioned character of coal tar, coal tar first carries out facing hydrogen cracking by the present invention, mainly scission reaction occurs.In a heated condition, the C-C bond rupture generation scission reaction that in alkane macromole, bond energy is less, generates alkane and the olefin hydrocarbon molecules of small-molecular-weight.Naphthenic hydrocarbon and aromatic hydrocarbons thermostability higher, at relatively high temperatures, five-ring, six-ring fracture generate alkene, benzene starts scission reaction occurs, as the polycyclic aromatic hydrocarbons such as naphthalene, anthracene also starts cracking.But because scission reaction is all carried out facing under hydrogen atmosphere, the direction of hydrocarbon cracking trend hydrotreated lube base oil and fracture is further carried out, thus 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 being reacted with hydrogen respectively generates hydrogen sulfide, ammonia and water.The light component oil fractionated out passes into hydrocracking tower further, aromatic hydrocarbons and long-chain macromolecule hydro carbons then respectively saturated and cracking generate short chain small molecules hydro carbons and naphthenic hydrocarbon, finally fractionate out in separation column meet that processed oil requirement, added value are high, clean, the gasoline of high-quality and diesel component.
The present invention compared with prior art tool has the following advantages: carry out cracking at hydro condition, and slow down or avoid the polycondensation generation generation coke of alkane, arene, the high value kind reduced 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 the on-stream time of cracking heating furnace device to greatest extent; Sulphur in coal tar, nitrogen, oxygen heteroatom can be removed more up hill and dale, improve the stability of hydrogenated products, significantly Improving The Quality of Products; Take into full account the compositing characteristic of full fraction of coal tar, when 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
The embodiment of coupling apparatus schema to this programme does description, and the present invention is described further.
Composition graphs 1, coal tar raw material 1 is entered cracking separation column 2, fractionate out the heavy component oil 3 being greater than 360 DEG C to enter cracking process furnace 6 and recycle, fractionate out the light component oil 4 being less than 360 DEG C and enter hydrofining operation, the heavy component oil 3 being preheated to 320 ~ 420 DEG C is mixed with hydrogen 5 and is sent to cracking process furnace 6, be heated to 400 ~ 480 DEG C and enter and face hydrogen cleavage column 7,8 and carry out scission reaction.Control cleavage column reaction pressure 0.28MPa in operation, temperature controls at 450 ~ 550 DEG C.Hydrogen-oil ratio controls: case 1 is 0; Case 2 is 20:1; Case 3 is 40:1.Two are faced hydrogen cleavage column 7,8 and operate for one-period switches by 18 hours or 24 hours, another cleaning residue 9 during a normal charging.
Eject the gas that comes from cleavage column and generate oil and 10 enter separator 11 through heat exchange, isolate dry gas 12, generate oil and enters cracking separation column 2 through cooling, heavy component oil 3 returns to enter into cleavage column process furnace 6 and faces hydrogen cleavage column 7,8 and again scission reaction occurs.
Light component oil 4 is mixed into hydrofining process furnace as the raw material of hydrogenation and part fresh hydrogen 13 or recycle hydrogen 14 and heats 15, and enter after mixing with another part fresh hydrogen 13 or recycle hydrogen 14 in hydrofining reactor 16, Special hydrogenation catalyst for refining is housed in hydrofining reactor.Control reaction stagnation pressure in operation is 8.0 ~ 18.0MPa, and average reaction temperature is 280 ~ 380 DEG C, 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, MoO
3be 15% ~ 30%, NiO be 2.0% ~ 4.5%, CeO be 2.5% ~ 4.5%, La
2o
3be 1.5% ~ 3.0%, F be 0.5% ~ 1.5%, all the other are Al
2o
3, 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, and intensity is greater than 120N/cm, and shape is trifolium, spherical or bar shaped.Under the effect of catalyzer, Hydrogenation raw oil medium sulphide content, nitride and oxide compound to react generation hydrogen sulfide with hydrogen respectively like this, ammonia and water, hydrofining high-pressure separator 17 is entered through heat exchange, 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 and heats through hydrocracking process furnace 22, and enter after mixing with another part fresh hydrogen 13 or recycle hydrogen 14 in hydrocracking reactor 23, Special hydrogenation cracking catalyst is housed in hydrocracking reactor.Control hydrofining reaction pressure in operation is specially 8.0 ~ 18.0MPa, and temperature of reaction is 300 ~ 400 DEG C, 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, WO
3be 10% ~ 32%, NiO be 3.0% ~ 4.3%, CoO be 2.0% ~ 3.8%, Nd
2o
3be 1.2% ~ 3.5%, P be 2.5% ~ 4.0%, all the other are Al
2o
3and beta-molecular sieve, pore volume is 0.3 ~ 0.36mL/g, and specific surface area is 100 ~ 300m
2/ g, tap density is 0.65 ~ 0.95g/mL, and intensity is greater than 120N/cm, and shape is 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, the further hydrotreated lube base oil of aromatic hydroxy compound open loop cracking, it is made to become micromolecular gasoline and diesel oil, hydrocracking high-pressure separator 24 is entered through heat exchange, 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.
It is of the present invention that to face hydrogen cracking technology different from the difference of raw material and production object.The main character of such as 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 composition is in table 3, and the main character of the product of case 2 is in table 4.
The main character of table 1 coal tar
Table 3 product material forms
The main character of table 4 product
Claims (9)
1. a coal tar faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil, it is characterized in that: the coal tar heavy duty component being greater than a certain temperature section of 360 DEG C that coal tar fractional distillation is obtained or without the full fraction of coal tar of any process as charging, in cleavage column, carry out scission reaction under hydro condition obtain cracking generation oil, then enter hydro-upgrading system and obtain gasoline and diesel oil;
Described combination process comprises the steps:
(1) coal tar is sent into cracking separation column after being preheated to 320 ~ 420 DEG C, fractionate out the heavy component oil being greater than 360 DEG C and the light component oil being less than 360 DEG C, light component oil enters hydrofining operation, heavy component oil is mixed with hydrogen, control hydrogen-oil ratio 0 ~ 200:1, be sent to process furnace to be again heated to 400 ~ 550 DEG C and to enter and face hydrogen cleavage column, it is that 0.1 ~ 3.0MPa carries out scission reaction that hydrogen cleavage column reaction pressure is faced in control, alkene under an atmosphere of hydrogen, aromatic hydrocarbons and other unsaturated hydro carbons polycondensation suppressed and reduce the incidence of coking, the residue produced after scission reaction is discharged continuously by facing at the bottom of hydrogen cleavage column, generate oil to export by facing hydrogen cracking tower top with dry gas, high-pressure separator is entered through heat exchange, isolate dry gas, generate oil and enter cracking separation column through cooling, heavy component oil returns into process furnace,
(2) light component oily mixing with part fresh hydrogen or recycle hydrogen heats through hydrofining process furnace, 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 DEG C, hydrogen-oil ratio 600 ~ 1200:1, volume space velocity 0.2 ~ 1.0h
-1under Hydrobon catalyst effect, make Hydrogenation raw oil medium sulphide content, nitride and oxide compound react with hydrogen respectively generate hydrogen sulfide, ammonia and water, hydrofining high-pressure separator is entered through heat exchange, isolating circulating hydrogen returns into reactor, isolated generation oil enters hydrogenation fractionating tower, isolates gasoline, diesel oil and tail oil;
(3) tail oil mixes with part fresh hydrogen or recycle hydrogen and heats through hydrocracking process furnace, 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 DEG C, 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, the further hydrotreated lube base oil of aromatic hydroxy compound open loop cracking, it is made to become micromolecular gasoline and diesel oil, hydrocracking high-pressure separator is entered through heat exchange, 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.
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: described coal tar refers to that the coal tar of coking by-product, the coal tar of gasification water gas by-product, coal tar extract phenol or/and residue cut after naphthalene.
3. coal tar as claimed in claim 1 faces the combination process of hydrogen cracking and hydro-upgrading made fuel oil, in described (1) process, it is characterized in that described hydrogen cleavage column reaction pressure of facing is 0.12 ~ 1.0MPa, hydrogen-oil ratio 0 ~ 60:1.
4. coal tar as claimed in claim 1 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 carries out the operation of cleaning residue.
5. coal tar as claimed in claim 1 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 warming temperature is specially 400 ~ 480 DEG C.
6. coal tar as claimed in claim 1 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 DEG C, hydrogen-oil ratio 800 ~ 1100:1, volume space velocity 0.2 ~ 0.8h
-1.
7. coal tar as claimed in claim 1 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, the main metal of its 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, MoO
3be 15% ~ 30%, NiO be 2.0% ~ 4.5%, CeO be 2.5% ~ 4.5%, La
2o
3be 1.5% ~ 3.0%, F be 0.5% ~ 1.5%, all the other are Al
2o
3, 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, and intensity is greater than 120N/cm, and shape is trifolium, spherical or bar shaped.
8. coal tar as claimed in claim 1 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 DEG C, hydrogen-oil ratio 1000 ~ 1200:1, volume space velocity 0.2 ~ 0.6h
-1.
9. coal tar as claimed in claim 1 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, the main metal of its 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, WO
3be 10% ~ 32%, NiO be 3.0% ~ 4.3%, CoO be 2.0% ~ 3.8%, Nd
2o
3be 1.2% ~ 3.5%, P be 2.5% ~ 4.0%, all the other are Al
2o
3and beta-molecular sieve, pore volume is 0.3 ~ 0.36mL/g, and specific surface area is 100 ~ 300m
2/ g, tap density is 0.65 ~ 0.95g/mL, and intensity is greater than 120N/cm, and shape is trifolium, spherical or bar shaped.
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| 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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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. |
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