CN109679674A - A kind of needle-shape coke raw material pretreating process - Google Patents
A kind of needle-shape coke raw material pretreating process Download PDFInfo
- Publication number
- CN109679674A CN109679674A CN201910030795.3A CN201910030795A CN109679674A CN 109679674 A CN109679674 A CN 109679674A CN 201910030795 A CN201910030795 A CN 201910030795A CN 109679674 A CN109679674 A CN 109679674A
- Authority
- CN
- China
- Prior art keywords
- solvent
- tower
- raw material
- tank
- pump
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of needle-shape coke raw material pretreating process, it include: slurry oil (1), raw material surge tank (2), high pressure solvent tank (3), extraction tower (4), supercritical recovery tower (5), vacuum pump line (6), deasphalted oil stripper (7), vacuum pump line (8), asphaltene stripper (9), solvent tank (10), carburet hydrogen (11), fresh solvent (12), desolvation agent (13), acid water (14), fresh water (15), raw material pumps (16), high-pressure solvent pump (17), move back oily line (18), diesel cycle line (19), rich aromatic naphtha (20), pitch (21), sewage pump (22), solvent (23) and static mixer (24), catalytic slurry is used to produce needle coke product for raw material, catalytic slurry first uses supercritical extract, it is enriched with it Middle aromatic component, then hydrogenated purification again, removes the impurity such as S, N therein, most produces needle coke through needle coke coking plant afterwards.
Description
Technical field
The present invention relates to a kind of processes of oil refining field needle-shape coke raw material preparation, refer in particular to oil system needle
The process of preparing of shape coke raw material.
Background technique
Needle coke is a kind of quality material in the carbon materials greatly developed the 1970s, and appearance is silver gray, has
The porosu solid of metallic luster, surface have lubrication to feel in apparent elongated needle-shaped or fibrous texture trend, internal holes it is big and
It is few, it is slightly ob-round, because its appearance has an apparent needle-shaped or fibrous texture structure, therefore referred to as needle coke (Needle
Coke), needle coke is with low thermal coefficient of expansion, low-porosity, low-sulfur, low ash point, low-metal content, high conductivity and Yi Shimo
The series of advantages such as change.The graphite product made of needle coke has high density, high intensity, high-purity, high-crystallinity, highly conductive
The features such as thermal conductivity, low thermal coefficient of expansion, low fever's corrosion, mainly for the production of electric furnace steel making high power, ultrahigh power graphite
Electrode production is used as high-energy neutron decelerating material in atomic pile, is also used in rocketry, wherein in metallurgical industry
Dosage is maximum.In metallurgical industry, when the ultra high power made of needle coke (UHP) graphite electrode can shorten electric furnace steel making smelting
Between 50~70%, power consumption can reduce by 30%, can improve efficiency significantly, reduce power consumption and raw materials consumption, reduce ring
Border pollution.Needle coke can be divided into petroleum needle coke and coal-based needle coke according to the difference of raw material.Due to the production of needle coke
Raw material and process conditions difference, performance is also not quite similar, but purposes is essentially identical.The main performance index of needle coke has very close
Degree, thermal expansion coefficient, ash content, sulfur content, nitrogen content, intensity, size distribution, resistivity and inoxidizability etc..It sees on the whole,
The quality of petroleum needle coke is better than coal-based needle coke, and price is also higher than coal-based needle coke by 10% or so.Needle coke in the world
Production technology is mainly monopolized by a few countries such as the U.S., Britain, Japan, Germany, in terms of Chinese steel industry development prospect, therefrom
State sees in big specification ultra high power graphite electrode production field strength at present, increases needle coke production technology and develops dynamics, makes excellent
The production domesticization of matter needle coke, not only can change China and produces big specification ultra high power graphite electrode status under one's control, and
It can also promote the development of China's steel and iron industry, a kind of prepare the one of high-quality needle-shape coke raw material in consideration of it, provided by the invention
Kind processing technology routine.
Summary of the invention
Purpose provided by the invention is to provide a kind of a kind of processing technology routine for preparing high-quality needle-shape coke raw material, packet
Include: slurry oil (1), high pressure solvent tank (3), extraction tower (4), supercritical recovery tower (5), vacuum pump line (6), takes off raw material surge tank (2)
Coal tar stripper (7), asphaltene stripper (9), solvent tank (10), carburet hydrogen (11), fresh solvent (12), moves back at vacuum pump line (8)
Solvent (13), fresh water (15), raw material pump (16), high-pressure solvent pump (17), moves back oily line (18), diesel cycle at acid water (14)
Line (19), rich aromatic naphtha (20), pitch (21), sewage pump (22), solvent (23) and static mixer (24), using catalytic slurry
Needle coke product is produced for raw material, catalytic slurry first uses supercritical extract, enrichment wherein aromatic component, then hydrogenated essence again
System, removes the impurity such as S, N therein, most produces needle coke, technical process through needle coke coking plant afterwards are as follows:
1. by tank field Lai catalytic slurry enter raw material surge tank (1) through Liquid level adjusting valve, raw material by raw material pump (16) extract out after
Enter static mixer (24) after feedstock oil goes into operation heater heating；
It goes into operation heater 2. solvent in high pressure solvent tank (3) is forced into after 1-6MPa extraction by high-pressure solvent pump (17) through solvent
Enter static mixer (24) after heating, enters in extraction tower (4) after being sufficiently mixed in static mixer (24) with slurry oil (1)
Portion, another way solvent (23) enter extraction tower (4) lower section and are further extracted oil therein；
3. most of aromatic naphtha phase hydro carbons is dissolved in solvent (23) in slurry oil (1), the lesser light phase of density is formed, and it is most of
Colloid, asphalitine do not dissolve in then solvent (23), formed the biggish heavy phase of density, weight two-phase in extraction tower respectively upwards, to
Lower flowing, heavy phase are finally settled down to extraction tower (4) bottom during decline, form light, weight two-phase in this way, and light phase is rich aromatic hydrocarbons
Oil solution, heavy phase are cold primer-oil；
4. overflowing the rich aromatic naphtha liquid phase containing a large amount of solvents at the top of from extraction tower (4), supercritical recovery is entered after heated heating
Tower (5)；
5. entering asphaltene stripper (9) after the cold primer-oil come out from extraction tower (4) bottom is heated, solvent is from asphaltene stripper
(9) top outflow, cold primer-oil are sent after the extraction cooling of asphaltene stripper (9) bottom to tank field；
6. in supercritical recovery tower (5), since the solubility of the rich aromatic naphtha of the raising of temperature in a solvent reduces, rich aromatic naphtha
It is separated with solvent, solvent enters high pressure solvent tank (17) after outflow cooling at the top of supercritical recovery tower (5)；
7. rich aromatic naphtha is from supercritical recovery tower (5) bottom, extraction enters deasphalted oil stripper (7), in deasphalted oil stripper
(7) in, since pressure declines, rich aromatic naphtha and solvent (23) are further separated, and solvent (23) is stripped from deasphalted oil
Outflow at the top of tower (7), cooling after being mixed with the solvent flowed out at the top of deasphalted oil stripper (7) to enter solvent tank (10), Fu Fang
Hydrocarbon ils is sent after cooling from the extraction of deasphalted oil stripper (7) bottom to tank field；
8. solvent (23) is mixed into high pressure solvent tank (3) through solvent pump (24) and supercritical recovery tower (5) top solvent recovery line,
It is recycled；
9. sewage pumps out workshop through sewage pump (22).
The vacuum pump line (6) is from extraction tower (4) tower top, supercritical recovery tower (5) tower top, deasphalted oil stripper (7)
Tower top and the extraction of asphaltene stripper (9) tower top, enter solvent tank (10) after collecting, the recycling design in the solvent tank (10)
Extraction tower (4) are returned after solvent pump (23) extraction.
Gaseous hydrocarbon (11) in the solvent tank (10) is by the outer discharger of solvent tank (10) overhead line, with stylish
Fresh solvent (12) enters solvent tank (10) by overhead line.
The pump discharge of the solvent pump (23) returns to high-pressure solvent pump (17) by moving back oily line, the solvent pump (23)
Another outlet by diesel cycle line (19) return extraction tower (4) feeding line.
Detailed description of the invention
Fig. 1 is process flow chart of the invention.
In appended drawing reference figure, 1 slurry oil, 2 raw material surge tanks, 3 high pressure solvent tanks, 4 extraction towers, 5 supercritical recovery towers, 6 are taken out
Ceases to be busy, 7 deasphalted oil strippers, 8 vacuum pump lines, 9 asphaltene strippers, 10 solvent tanks, 11 carburet hydrogens, 12 fresh solvents, 13 desolvations
Agent, 14 acid waters, 15 fresh waters, 16 raw materials pump, 17 high-pressure solvent pumps, 18 move back oily line, 19 diesel cycle lines, 20 rich aromatic naphtha,
21 pitches, 22 sewage pumps, 23 solvents, 24 static mixers
Specific embodiment
Below by a kind of preparation side of specific embodiment orderly mesophase needle coke that present invention be described in more detail
Method, those skilled in the art is after having read this specific embodiment, it is to be understood that and implement technical solutions according to the invention,
Excellent effect described in it can also be embodied by specific embodiment.
Embodiment
This method is similar to the true boiling point distillation of crude oil, using the dissolubility property of lighter hydrocarbons solvent in the supercritical state,
Dare matter oil by all kinds of and efficiently separate.The advantage is that: separation temperature is low (< 250 DEG C), extracting rate is high, can obtain more
A narrow fraction, and its separation principle is similar to the solvent extraction of industry, and result of study has practical value, and this method can have
Effect ground separation catalytic slurry.
1. by tank field Lai catalytic slurry enter raw material surge tank (1) through Liquid level adjusting valve, raw material by raw material pump (16) take out
Enter static mixer (24) after feedstock oil goes into operation heater heating after out；
It goes into operation heater 2. solvent in high pressure solvent tank (3) is forced into after 1-6MPa extraction by high-pressure solvent pump (17) through solvent
Enter static mixer (24) after heating, enters in extraction tower (4) after being sufficiently mixed in static mixer (24) with slurry oil (1)
Portion, another way solvent (23) enter extraction tower (4) lower section and are further extracted oil therein；
3. most of aromatic naphtha phase hydro carbons is dissolved in solvent (23) in slurry oil (1), the lesser light phase of density is formed, and it is most of
Colloid, asphalitine do not dissolve in then solvent (23), formed the biggish heavy phase of density, weight two-phase in extraction tower respectively upwards, to
Lower flowing, heavy phase are finally settled down to extraction tower (4) bottom during decline, form light, weight two-phase in this way, and light phase is rich aromatic hydrocarbons
Oil solution, heavy phase are cold primer-oil；
4. overflowing the rich aromatic naphtha liquid phase containing a large amount of solvents at the top of from extraction tower (4), supercritical recovery is entered after heated heating
Tower (5)；
5. entering asphaltene stripper (9) after the cold primer-oil come out from extraction tower (4) bottom is heated, solvent is from asphaltene stripper
(9) top outflow, cold primer-oil are sent after the extraction cooling of asphaltene stripper (9) bottom to tank field；
6. in supercritical recovery tower (5), since the solubility of the rich aromatic naphtha of the raising of temperature in a solvent reduces, rich aromatic naphtha
It is separated with solvent, solvent enters high pressure solvent tank (17) after outflow cooling at the top of supercritical recovery tower (5)；
7. rich aromatic naphtha is from supercritical recovery tower (5) bottom, extraction enters deasphalted oil stripper (7), in deasphalted oil stripper
(7) in, since pressure declines, rich aromatic naphtha and solvent (23) are further separated, and solvent (23) is stripped from deasphalted oil
Outflow at the top of tower (7), cooling after being mixed with the solvent flowed out at the top of deasphalted oil stripper (7) to enter solvent tank (10), Fu Fang
Hydrocarbon ils is sent after cooling from the extraction of deasphalted oil stripper (7) bottom to tank field；
8. solvent (23) is mixed into high pressure solvent tank (3) through solvent pump (24) and supercritical recovery tower (5) top solvent recovery line,
It is recycled；
9. sewage pumps out workshop through sewage pump (22).
The vacuum pump line (6) is from extraction tower (4) tower top, supercritical recovery tower (5) tower top, deasphalted oil stripper (7)
Tower top and the extraction of asphaltene stripper (9) tower top, enter solvent tank (10) after collecting, the recycling design in the solvent tank (10)
Extraction tower (4) are returned after solvent pump (23) extraction.
Gaseous hydrocarbon (11) in the solvent tank (10) is by the outer discharger of solvent tank (10) overhead line, with stylish
Fresh solvent (12) enters solvent tank (10) by overhead line.
The pump discharge of the solvent pump (23) returns to high-pressure solvent pump (17) by moving back oily line, the solvent pump (23)
Another outlet by diesel cycle line (19) return extraction tower (4) feeding line.
Claims (4)
1. a kind of needle-shape coke raw material pretreating process, comprising: slurry oil (1), raw material surge tank (2), high pressure solvent tank (3), extracting
It is tower (4), supercritical recovery tower (5), vacuum pump line (6), deasphalted oil stripper (7), vacuum pump line (8), asphaltene stripper (9), molten
Agent tank (10), carburet hydrogen (11), fresh solvent (12), desolvation agent (13), acid water (14), fresh water (15), raw material pump (16),
High-pressure solvent pump (17) moves back oily line (18), is diesel cycle line (19), rich aromatic naphtha (20), pitch (21), sewage pump (22), molten
Agent (23) and static mixer (24) use catalytic slurry to produce needle coke product for raw material, and catalytic slurry first uses overcritical
Extraction is enriched with wherein aromatic component, and then hydrogenated purification again, removes the impurity such as S, N therein, most fills afterwards through needle coke coking
Set production needle coke, technical process are as follows:
1. by tank field Lai catalytic slurry enter raw material surge tank (1) through Liquid level adjusting valve, raw material by raw material pump (16) extract out after
Enter static mixer (24) after feedstock oil goes into operation heater heating；
It goes into operation heater 2. solvent in high pressure solvent tank (3) is forced into after 1-6MPa extraction by high-pressure solvent pump (17) through solvent
Enter static mixer (24) after heating, enters in extraction tower (4) after being sufficiently mixed in static mixer (24) with slurry oil (1)
Portion, another way solvent (23) enter extraction tower (4) lower section and are further extracted oil therein；
3. most of aromatic naphtha phase hydro carbons is dissolved in solvent (23) in slurry oil (1), the lesser light phase of density is formed, and it is most of
Colloid, asphalitine do not dissolve in then solvent (23), formed the biggish heavy phase of density, weight two-phase in extraction tower respectively upwards, to
Lower flowing, heavy phase are finally settled down to extraction tower (4) bottom during decline, form light, weight two-phase in this way, and light phase is rich aromatic hydrocarbons
Oil solution, heavy phase are cold primer-oil；
4. overflowing the rich aromatic naphtha liquid phase containing a large amount of solvents at the top of from extraction tower (4), supercritical recovery is entered after heated heating
Tower (5)；
5. entering asphaltene stripper (9) after the cold primer-oil come out from extraction tower (4) bottom is heated, solvent is from asphaltene stripper
(9) top outflow, cold primer-oil are sent after the extraction cooling of asphaltene stripper (9) bottom to tank field；
6. in supercritical recovery tower (5), since the solubility of the rich aromatic naphtha of the raising of temperature in a solvent reduces, rich aromatic naphtha
It is separated with solvent, solvent enters high pressure solvent tank (17) after outflow cooling at the top of supercritical recovery tower (5)；
7. rich aromatic naphtha is from supercritical recovery tower (5) bottom, extraction enters deasphalted oil stripper (7), in deasphalted oil stripper
(7) in, since pressure declines, rich aromatic naphtha and solvent (23) are further separated, and solvent (23) is stripped from deasphalted oil
Outflow at the top of tower (7), cooling after being mixed with the solvent flowed out at the top of deasphalted oil stripper (7) to enter solvent tank (10), Fu Fang
Hydrocarbon ils is sent after cooling from the extraction of deasphalted oil stripper (7) bottom to tank field；
8. solvent (23) is mixed into high pressure solvent tank (3) through solvent pump (24) and supercritical recovery tower (5) top solvent recovery line,
It is recycled；
9. sewage pumps out workshop through sewage pump (22).
2. a kind of needle-shape coke raw material pretreating process according to claim 1, it is characterised in that: the vacuum pump line (6)
From extraction tower (4) tower top, supercritical recovery tower (5) tower top, deasphalted oil stripper (7) tower top and asphaltene stripper (9) tower top
Extraction enters solvent tank (10) after collecting, and the recycling design in the solvent tank (10) returns after solvent pump (23) extraction
Pumpback stripper (4).
3. a kind of needle-shape coke raw material pretreating process according to claim 1, it is characterised in that: the solvent tank (10)
In gaseous hydrocarbon (11) by the outer discharger of solvent tank (10) overhead line, while fresh solvent (12) by overhead line into
Enter solvent tank (10).
4. a kind of needle-shape coke raw material pretreating process according to claim 1, it is characterised in that: the solvent pump (23)
Pump discharge return to high-pressure solvent pump (17) by moving back oily line, another outlet of the solvent pump (23) passes through diesel cycle
Line (19) returns to extraction tower (4) feeding line.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910011115 | 2019-01-07 | ||
| CN2019100111153 | 2019-01-07 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109679674A true CN109679674A (en) | 2019-04-26 |
Family
ID=66193142
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910030795.3A Pending CN109679674A (en) | 2019-01-07 | 2019-01-14 | A kind of needle-shape coke raw material pretreating process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109679674A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110511785A (en) * | 2019-09-20 | 2019-11-29 | 黄河三角洲京博化工研究院有限公司 | A method of needle-shape coke raw material oil is prepared using slurry oil |
| CN111961498A (en) * | 2020-08-13 | 2020-11-20 | 山东益大新材料股份有限公司 | Multiphase step heavy oil separation process and application of product thereof |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2232792C2 (en) * | 2002-09-27 | 2004-07-20 | Государственное унитарное предприятие "Институт нефтехимпереработки" | Petroleum residue deasphalting process |
| CN1891784A (en) * | 2005-07-05 | 2007-01-10 | 中国石油大学(北京) | Method for realizing heavy oil deep-step separation by coupled residue granulating |
| CN102690678A (en) * | 2011-03-24 | 2012-09-26 | 中国石油化工股份有限公司 | Processing method of inferior heavy crude oil |
| CN105400545A (en) * | 2014-09-10 | 2016-03-16 | 中国石油大学(北京) | Heavy oil separation method and treatment system thereof |
| CN105482850A (en) * | 2016-01-12 | 2016-04-13 | 广西泓达生物能源科技有限公司 | System device for producing needle coke crude oil through catalytic slurry oil |
| CN108102710A (en) * | 2016-11-25 | 2018-06-01 | 中国石油化工股份有限公司 | A kind of method for preparing needle coke |
| CN108893140A (en) * | 2018-06-05 | 2018-11-27 | 山东益大新材料有限公司 | A method of branded oil system needle-shape coke raw material is produced by solvent separation and Extraction |
-
2019
- 2019-01-14 CN CN201910030795.3A patent/CN109679674A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2232792C2 (en) * | 2002-09-27 | 2004-07-20 | Государственное унитарное предприятие "Институт нефтехимпереработки" | Petroleum residue deasphalting process |
| CN1891784A (en) * | 2005-07-05 | 2007-01-10 | 中国石油大学(北京) | Method for realizing heavy oil deep-step separation by coupled residue granulating |
| CN102690678A (en) * | 2011-03-24 | 2012-09-26 | 中国石油化工股份有限公司 | Processing method of inferior heavy crude oil |
| CN105400545A (en) * | 2014-09-10 | 2016-03-16 | 中国石油大学(北京) | Heavy oil separation method and treatment system thereof |
| CN105482850A (en) * | 2016-01-12 | 2016-04-13 | 广西泓达生物能源科技有限公司 | System device for producing needle coke crude oil through catalytic slurry oil |
| CN108102710A (en) * | 2016-11-25 | 2018-06-01 | 中国石油化工股份有限公司 | A kind of method for preparing needle coke |
| CN108893140A (en) * | 2018-06-05 | 2018-11-27 | 山东益大新材料有限公司 | A method of branded oil system needle-shape coke raw material is produced by solvent separation and Extraction |
Non-Patent Citations (1)
| Title |
|---|
| 中国石油大学（北京）重质油国家重点实验室: "针焦原料超临界萃取分离装置设计说明", 《针焦原料超临界萃取分离装置设计说明》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110511785A (en) * | 2019-09-20 | 2019-11-29 | 黄河三角洲京博化工研究院有限公司 | A method of needle-shape coke raw material oil is prepared using slurry oil |
| CN111961498A (en) * | 2020-08-13 | 2020-11-20 | 山东益大新材料股份有限公司 | Multiphase step heavy oil separation process and application of product thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101289625B (en) | Production process of dipping agent bitumen | |
| US10752850B2 (en) | Combined hydrogenation process method for producing high-quality fuel by medium-low-temperature coal tar | |
| CN104962307B (en) | Method for producing light oil through coal liquefaction | |
| CN102021005B (en) | Method for producing needle coke | |
| CN109679674A (en) | A kind of needle-shape coke raw material pretreating process | |
| CN106883871B (en) | A kind of production method of needle-shape coke raw material | |
| CN106147834A (en) | A kind of combined method separating catalytic cracked oil pulp and preparing mesophase pitch | |
| CN105482850A (en) | System device for producing needle coke crude oil through catalytic slurry oil | |
| WO2012174860A1 (en) | Device and method for low-cost production of low-sulphur, high-octane gasoline | |
| CN103102932B (en) | Hydrocarbon modification separation method | |
| CN108893140B (en) | Method for producing high-quality oil-based needle coke raw material through solvent separation and extraction | |
| CN208346102U (en) | The pretreatment of raw material solvent extraction system of needle coke industrialized production | |
| CN114806620B (en) | Pretreatment process for preparing raw materials from coal-based needle coke | |
| DE112011101330B4 (en) | Method and apparatus for the liquefaction and distillation of volatiles of carbonaceous solids | |
| CN105713647B (en) | A kind of utilization coal tar maximization prepares the method and device of carbolic oil and diesel oil | |
| CN109054878A (en) | A method of adding hydrogen to produce oil by aromatic naphtha is needle-shape coke raw material | |
| CN215995647U (en) | Take oily furfural cyclic processing device | |
| CN108264931A (en) | For producing the separator of refined bitumen tempered oil | |
| CN109370627B (en) | Solvent for preparing high-quality coal-based needle coke, preparation method and application thereof | |
| CN208104301U (en) | Asphaltene precipitation heavy phase system injects the device that carbolineum extends the system cycle of operation | |
| CN1055303C (en) | Reusing method for extracted solution of lubricating oil solvent | |
| CN1382761A (en) | Process for preparing acicular coke by catalytic cracking of classified oil | |
| CN108395904B (en) | Raw material pretreatment solvent extraction system and method for needle coke industrial production | |
| CN102443408B (en) | Pressure reduction distillation process method | |
| CN205473603U (en) | Catalysis slurry oil production needle coke raw oil system device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20190426 |