CN103242880A - High-quality impregnant asphalt production process - Google Patents
High-quality impregnant asphalt production process Download PDFInfo
- Publication number
- CN103242880A CN103242880A CN2013101664096A CN201310166409A CN103242880A CN 103242880 A CN103242880 A CN 103242880A CN 2013101664096 A CN2013101664096 A CN 2013101664096A CN 201310166409 A CN201310166409 A CN 201310166409A CN 103242880 A CN103242880 A CN 103242880A
- Authority
- CN
- China
- Prior art keywords
- subsider
- solvent
- quality
- vacuum still
- production technique
- 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.)
- Granted
Links
Images
Landscapes
- Working-Up Tar And Pitch (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a high-quality impregnant asphalt production process. The high-quality impregnant asphalt production process is characterized by comprising the following steps of: mixing first solvent coal oil and second solvent washing oil for extraction by using a pipeline mixer, and then feeding the mixture into a stirring tank; feeding raw material coal asphalt into the stirring tank for stirring; pumping the stirred raw material coal asphalt into a first settling tank through an oil pump; pumping a heavy phase part in the first settling tank into a quinoline insoluble centrifugal removal device through the oil pump, and centrifugally removing quinoline insoluble residue; returning a material from which the quinoline insoluble residue is removed into the first settling tank; when the storage amount of mixed liquid in the first settling tank reaches the limit, enabling the mixed liquid to enter into a second settling tank, and standing; after lamination occurs in the second settling tank, heating a light phase component in the second settling tank through a first heating furnace, and pumping the light phase component into a first depressurizing distillation tower for depressurizing distillation; and removing a solvent, and thus obtaining a target product, namely high-quality impregnant asphalt. The high-quality impregnant asphalt production process is used for producing the high-quality impregnant asphalt. The product yield is high and can exceed 60 percent. The temperature of a softening point of a product is 70 to 90 DEG C. The ash content can be controlled to be 0.01 to 0.1 percent.
Description
Technical field
This patent relates to Coal Chemical Industry industry coal-tar pitch product deep processing field, is specifically related to a kind of high-quality dipping agent bitumen production technique.
Background technology
In the Coal Chemical Industry industry, the coal-tar pitch product mostly is low-end product, and added value is low, produces high-quality coal-tar pitch product and can make the coal-tar pitch added value of product improve several times.At present, high-quality dipping agent bitumen production technique mainly contains following several: 1, filtering separation method; 2, centrifugal separation; 3, solvent extration.But it is reported that filtering separation method and centrifugal separation are for producing high-quality coal-tar pitch product at present, technology is immature, and the technical barrier of existence also is not resolved.Therefore mostly existing production technique for the production of high-quality dipping agent bitumen is to adopt solvent extration, but its high-quality coal-tar pitch quality product of producing is relatively poor, and yield is not high yet.This mainly is because it can not remove the impurity in the deasphalting effectively, thus restive pitch ash content.
Summary of the invention:
Technical problem to be solved by this invention is to provide a kind of high-quality dipping agent bitumen production technique.
For solving the problems of the technologies described above the technical solution used in the present invention:
High-quality dipping agent bitumen production technique, it is characterized in that: it may further comprise the steps:
To extract and send into steel basin after mixing with line mixer with the first solvent kerosene and the second solvent washing oil, simultaneously feed coal pitch is sent in the steel basin and stirred, be pumped into first subsider by oil pump, and the heavy phase in first subsider part is pumped into through oil pump quinoline insolubles is centrifugal to be removed in the device, centrifugal removal quinoline insolubles slag removes loopback of material behind the quinoline insolubles slag in first subsider;
After the mixed solution storage capacity in first subsider reaches limit, can enter second subsider by flowing full, leave standstill, after treating layering to occur in second subsider, light phase component in second subsider is pumped into first vacuum still carry out underpressure distillation after first process furnace heats, remove solvent and obtain the high-quality dipping agent bitumen of target product.
Press such scheme, described extraction is 1:1.6～2 with the first solvent kerosene with the mass ratio that extracts with the second solvent washing oil, and the mass ratio of described raw material and extraction solvent is 1:1.5～2.5.
Press such scheme, described quinoline insolubles is centrifugal to remove the slag bucket that device comprises ultracentrifuge and links to each other with ultracentrifuge, is used for collecting the quinoline insolubles slag that removes.
Press such scheme, the time of repose of mixed solution is 6～8h in described second subsider.
Press such scheme, light phase component in described second subsider is heated to 320～350 ℃ through first process furnace, send into first vacuum still then and carry out underpressure distillation, the underpressure distillation condition of first vacuum still is: 20～60KPa(absolute pressure), column bottom temperature is at 300～320 ℃.
Press such scheme, after it also is included in and layering occurs in second subsider, the heavy phase component in second subsider after second process furnace heats, is pumped into second vacuum still and carries out underpressure distillation, remove solvent and heavy oil, obtain hard pitch.
Press such scheme, heavy phase component in described second subsider is heated to 340～370 ℃ through second process furnace, send into second vacuum still then and carry out underpressure distillation, the underpressure distillation condition of second vacuum still is: 20～60KPa(absolute pressure), 290 ± 5 ℃ of the tower temperature outs of heavy oil, column bottom temperature is at 320～340 ℃.
Press such scheme, the solvent that the solvent that the described second vacuum still top removes and the first vacuum still top remove is joined use through sending into after the condenser condenses to return after the cut groove is handled.
This high-quality dipping agent bitumen production technique is passed through solvent extration, standing sedimentation method and centrifugal separation organically combine, namely will extract earlier with solvent compounding in advance, then with raw material in steel basin behind the mixed dissolution, transfer in first subsider, at the same time, the heavy phase of natural subsidence in first subsider is pumped into partly quinoline insolubles is centrifugal to be removed in the device through the centrifugal quinoline insolubles slag that removes, can be back in first subsider more then, this has solved independent raw material on the one hand and has carried out the very difficult problem of centrifugation, on the other hand also owing to the quinoline insolubles of having removed in advance in the feed coal pitch, so compare with simple solvent extration, quality product also can be controlled well.Can go in second subsider by flowing full after the mixed solution of first subsider reaches limit further, the low mid-boiling point component solution (hereinafter to be referred as light phase) in that this extraction obtains after the underpressure distillation desolventizing, obtains high-quality dipping agent bitumen.Simultaneously, also the heavy hydrocarbon component (hereinafter to be referred as heavy phase) in second subsider can be removed at the bottom of tower through underpressure distillation, produce the byproduct hard pitch.Meanwhile, the lightweight solvent oil content that vacuum still steams also can be got back to steel basin after the cut groove is handled through sending into after the condenser condenses, returns and joins use.Particularly, select for use kerosene and washing oil to mix as the extraction mixed solvent, its major cause is that coal-tar pitch is mainly aromatic series macromole ring-type component, and the washing oil in the mixed solvent is based on aromatic hydrocarbons, strong to the coal-tar pitch dissolving power, but its density is big, and the viscosity height is unfavorable for the settlement separate of quinoline insolubles (QI) particle.And the main component in the kerosene is various alkanes, and is relatively poor with the intermiscibility of feed coal pitch, but its density is little, viscosity is low, and according to Stokes'theorem, it is conducive to the settlement separate of quinoline insolubles (QI) QI particle; Particularly utilize the characteristic of alkanes solubility property difference, can form the residue of q.s, these insoluble slags can be taken the tiny QI particle that is difficult in the pitch remove out of when settlement separate together, thereby reach the purpose that thoroughly removes small QI particle.In addition, consider that washing oil is aromatic solvent, improve the washing oil consumption, can improve the solvability of pitch, the pitch solubility property improves, and the refined asphaltic bitumen yield must increase.Comprehensively obtain by experiment at last: two kinds of solvent quality of washing oil and kerosene are under the situation of 1.5-2.5:1 than arriving 1.6-2:1, solvent and raw material ratio, refined asphaltic bitumen recovering effect the best.
Beneficial effect of the present invention:
Technology of the present invention is for the production of high-quality dipping agent bitumen, product yield height (can reach more than 60%), and the product softening temperature is at 70～90 ℃, and ash content can be controlled in 0.01～0.1%.
Description of drawings
Fig. 1 is high-quality dipping agent bitumen production equipment synoptic diagram in the embodiment of the invention.Among the figure: 1-solvent trough, 2-steel basin, 3-line mixer, 4-first subsider, 5-second subsider, 6-slag bucket, 7-ultracentrifuge, 8-first process furnace, 9-first vacuum still, 10-second vacuum still, 11-condenser, 12-second process furnace, 13-first oil pump, 14-second oil pump, 15-the 3rd oil pump, 16-the 4th oil pump.
Embodiment
Embodiment 1
As shown in Figure 1: the production technique of high-quality dipping agent bitumen, it is to send into steel basin 2 with being stored in after extraction in the solvent trough 1 mixes with line mixer 3 in the ratio of mass ratio 1:1.6 with the first solvent kerosene and the second solvent washing oil, simultaneously feed coal pitch is sent in the steel basin and stirred, the mass ratio of feed coal pitch and extraction solvent is 1:1.5, be pumped into first subsider 4 by first oil pump 13, and the heavy phase in first subsider part is pumped into through second oil pump 14 quinoline insolubles is centrifugal to be removed in the device, the centrifugal device that removes of described quinoline insolubles comprises ultracentrifuge 7 and the slag bucket 8 that links to each other with ultracentrifuge, by the centrifugal removal quinoline insolubles of ultracentrifuge slag, the quinoline insolubles slag that removes is collected in the slag bucket, removes loopback of material behind the quinoline insolubles slag in first subsider;
After the mixed solution storage capacity in first subsider reaches limit, can enter second subsider 5 by flowing full, leave standstill 6h, after treating layering to occur in second subsider, light phase component in second subsider is heated to 320 ℃ through first process furnace 8 to be pumped into first vacuum still 9 by the 3rd oil pump 15 and carries out underpressure distillation, the underpressure distillation condition of first vacuum still is: 20 KPa(absolute pressures), column bottom temperature removes solvent and obtains the high-quality dipping agent bitumen of target product at 300 ℃; Heavy phase component in second subsider is heated to 340 ℃ through second process furnace 12 to be pumped into second vacuum still 10 by the 4th oil pump 16 and carries out underpressure distillation, the underpressure distillation condition of second vacuum still is: the 20KPa(absolute pressure), 290 ± 5 ℃ of the tower temperature outs of heavy oil, column bottom temperature is at 320 ℃, remove solvent and heavy oil, obtain hard pitch; The solvent that described second vacuum still and the first vacuum still top remove can be sent into to return after the cut groove is handled and join use then through condenser 11 condensations.
The dipping agent bitumen product yield can reach more than 60%, softening temperature about 85 ℃, ash content about 0.06%.
The production technique of high-quality dipping agent bitumen, it is to send into steel basin 2 with being stored in after extraction in the solvent trough 1 mixes with line mixer 3 in the ratio of mass ratio 1:2 with the first solvent kerosene and the second solvent washing oil, simultaneously feed coal pitch is sent in the steel basin and stirred, the mass ratio of feed coal pitch and extraction solvent is 1:2, be pumped into first subsider 4 by first oil pump 13, and the heavy phase in first subsider part is pumped into through two oil pumps 14 quinoline insolubles is centrifugal to be removed in the device, the centrifugal device that removes of described quinoline insolubles comprises ultracentrifuge 7 and the slag bucket 8 that links to each other with ultracentrifuge, by the centrifugal removal quinoline insolubles of ultracentrifuge slag, the quinoline insolubles slag that removes is collected in the slag bucket, removes loopback of material behind the quinoline insolubles slag in first subsider;
After the mixed solution storage capacity in first subsider reaches limit, can enter second subsider 5 by flowing full, leave standstill 8h, after treating layering to occur in second subsider, light phase component in second subsider is heated to 340 ℃ through first process furnace 8 to be pumped into first vacuum still 9 by the 3rd oil pump 15 and carries out underpressure distillation, the underpressure distillation condition of first vacuum still is: the 60KPa(absolute pressure), column bottom temperature removes solvent and obtains the high-quality dipping agent bitumen of target product at 320 ℃; With the heavy phase component in second subsider after second process furnace 12 is heated to 370 ℃, pump into second vacuum still 10 through the 4th oil pump 16 and carry out underpressure distillation, the underpressure distillation condition is: the underpressure distillation condition of second vacuum still is: the 60KPa(absolute pressure), 290 ± 5 ℃ of the tower temperature outs of heavy oil, column bottom temperature is at 340 ℃, remove solvent and heavy oil, obtain hard pitch.The solvent that described second vacuum still and the first vacuum still top remove can be sent into to return after the cut groove is handled and join use then through condenser 11 condensations.
The dipping agent bitumen product yield can reach more than 60%, softening temperature about 90 ℃, ash content about 0.06%.
Claims (8)
1. high-quality dipping agent bitumen production technique, it is characterized in that: it may further comprise the steps: will extract and send into steel basin after mixing with line mixer with the first solvent kerosene and the second solvent washing oil, simultaneously feed coal pitch is sent in the steel basin and stirred, be pumped into first subsider by oil pump, and the heavy phase in first subsider part is pumped into through oil pump quinoline insolubles is centrifugal to be removed in the device, centrifugal removal quinoline insolubles slag removes loopback of material behind the quinoline insolubles slag in first subsider;
After the mixed solution storage capacity in first subsider reaches limit, can enter second subsider by flowing full, leave standstill, after treating layering to occur in second subsider, light phase component in second subsider is pumped into first vacuum still carry out underpressure distillation after first process furnace heats, remove solvent and obtain the high-quality dipping agent bitumen of target product.
2. high-quality dipping agent bitumen production technique according to claim 1, it is characterized in that: described extraction is 1:1.6～2 with the first solvent kerosene with the mass ratio that extracts with the second solvent washing oil, and the mass ratio of described raw material and extraction solvent is 1:1.5～2.5.
3. high-quality dipping agent bitumen production technique according to claim 1 is characterized in that: described quinoline insolubles is centrifugal to remove the slag bucket that device comprises ultracentrifuge and links to each other with ultracentrifuge, is used for collecting the quinoline insolubles slag that removes.
4. high-quality dipping agent bitumen production technique according to claim 1, it is characterized in that: the time of repose of mixed solution is 6～8h in described second subsider.
5. high-quality dipping agent bitumen production technique according to claim 1, it is characterized in that: the light phase component in described second subsider is heated to 320～350 ℃ through first process furnace, send into first vacuum still then and carry out underpressure distillation, the underpressure distillation condition of first vacuum still is: 20～60KPa(absolute pressure), column bottom temperature is at 300～320 ℃.
6. high-quality dipping agent bitumen production technique according to claim 1, it is characterized in that: after it also is included in and layering occurs in second subsider, with the heavy phase component in second subsider after second process furnace heats, pump into second vacuum still and carry out underpressure distillation, remove solvent and heavy oil, obtain hard pitch.
7. high-quality dipping agent bitumen production technique according to claim 6, it is characterized in that: the heavy phase component in described second subsider is heated to 340～370 ℃ through second process furnace, send into second vacuum still then and carry out underpressure distillation, the underpressure distillation condition of second vacuum still is: 20～60KPa(absolute pressure), 290 ± 5 ℃ of the tower temperature outs of heavy oil, column bottom temperature is at 320～340 ℃.
8. high-quality dipping agent bitumen production technique according to claim 1, it is characterized in that: the solvent that the solvent that the described second vacuum still top removes and the first vacuum still top remove is joined use through sending into after the condenser condenses to return after the cut groove is handled.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310166409.6A CN103242880B (en) | 2013-05-08 | 2013-05-08 | High-quality impregnant asphalt production process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310166409.6A CN103242880B (en) | 2013-05-08 | 2013-05-08 | High-quality impregnant asphalt production process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103242880A true CN103242880A (en) | 2013-08-14 |
| CN103242880B CN103242880B (en) | 2014-11-19 |
Family
ID=48922762
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310166409.6A Expired - Fee Related CN103242880B (en) | 2013-05-08 | 2013-05-08 | High-quality impregnant asphalt production process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103242880B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105754630A (en) * | 2016-03-25 | 2016-07-13 | 神华集团有限责任公司 | Preparation method of coal liquefied asphalt |
| CN107937010A (en) * | 2017-11-21 | 2018-04-20 | 七台河宝泰隆圣迈煤化工有限责任公司 | Densimetry instructs solvent extraction continuous sedimentation pitch pretreating process circulation solvent to return the method matched somebody with somebody |
| CN109518230A (en) * | 2019-01-21 | 2019-03-26 | 中南大学 | A kind of encryption anode carbon block impregnating agent and preparation method thereof |
| CN111218294A (en) * | 2018-11-27 | 2020-06-02 | 宝武炭材料科技有限公司 | Method for purifying quinoline insoluble coal-series asphalt with high softening point and high softening point |
| CN111363577A (en) * | 2020-03-12 | 2020-07-03 | 中国科学院山西煤炭化学研究所 | Spinnable asphalt for coal-based general-grade asphalt carbon fibers and preparation method thereof |
| CN115197733A (en) * | 2022-06-29 | 2022-10-18 | 鞍钢化学科技有限公司 | Low-QI impregnant asphalt preparation system and process |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4278529A (en) * | 1980-06-30 | 1981-07-14 | Kerr-Mcgee Refining Corporation | Process for separating bituminous materials with solvent recovery |
| US5066384A (en) * | 1985-02-28 | 1991-11-19 | Sumitomo Metal Industries, Ltd. | Process for refining coal-derived heavy carbonaceous materials |
| CN1724611A (en) * | 2005-07-19 | 2006-01-25 | 上海应用技术学院 | Preparation method of needle coke |
| US20080017549A1 (en) * | 2006-05-24 | 2008-01-24 | Kennel Elliot B | Method of producing synthetic pitch |
| CN101445740A (en) * | 2009-01-04 | 2009-06-03 | 北京石油化工学院 | A preparation method of dipping agent pitch |
| CN101508903A (en) * | 2009-03-20 | 2009-08-19 | 上海宝钢化工有限公司 | Process for continuously removing quinoline insoluble substances in coal tar pitch |
| CN101724424A (en) * | 2008-10-21 | 2010-06-09 | 上海宝钢化工有限公司 | Method for purifying maltha by using solvent deposition method |
| CN101824329A (en) * | 2010-05-17 | 2010-09-08 | 朱兴建 | Novel process for eliminating quinoline insoluble substances in coal tar medium temperature pitch |
| CN102051191A (en) * | 2009-11-03 | 2011-05-11 | 上海宝钢化工有限公司 | Production method and system of coal-based needle coke |
-
2013
- 2013-05-08 CN CN201310166409.6A patent/CN103242880B/en not_active Expired - Fee Related
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4278529A (en) * | 1980-06-30 | 1981-07-14 | Kerr-Mcgee Refining Corporation | Process for separating bituminous materials with solvent recovery |
| US5066384A (en) * | 1985-02-28 | 1991-11-19 | Sumitomo Metal Industries, Ltd. | Process for refining coal-derived heavy carbonaceous materials |
| CN1724611A (en) * | 2005-07-19 | 2006-01-25 | 上海应用技术学院 | Preparation method of needle coke |
| US20080017549A1 (en) * | 2006-05-24 | 2008-01-24 | Kennel Elliot B | Method of producing synthetic pitch |
| CN101724424A (en) * | 2008-10-21 | 2010-06-09 | 上海宝钢化工有限公司 | Method for purifying maltha by using solvent deposition method |
| CN101445740A (en) * | 2009-01-04 | 2009-06-03 | 北京石油化工学院 | A preparation method of dipping agent pitch |
| CN101508903A (en) * | 2009-03-20 | 2009-08-19 | 上海宝钢化工有限公司 | Process for continuously removing quinoline insoluble substances in coal tar pitch |
| CN102051191A (en) * | 2009-11-03 | 2011-05-11 | 上海宝钢化工有限公司 | Production method and system of coal-based needle coke |
| CN101824329A (en) * | 2010-05-17 | 2010-09-08 | 朱兴建 | Novel process for eliminating quinoline insoluble substances in coal tar medium temperature pitch |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105754630A (en) * | 2016-03-25 | 2016-07-13 | 神华集团有限责任公司 | Preparation method of coal liquefied asphalt |
| CN107937010A (en) * | 2017-11-21 | 2018-04-20 | 七台河宝泰隆圣迈煤化工有限责任公司 | Densimetry instructs solvent extraction continuous sedimentation pitch pretreating process circulation solvent to return the method matched somebody with somebody |
| CN111218294A (en) * | 2018-11-27 | 2020-06-02 | 宝武炭材料科技有限公司 | Method for purifying quinoline insoluble coal-series asphalt with high softening point and high softening point |
| CN111218294B (en) * | 2018-11-27 | 2021-07-23 | 宝武炭材料科技有限公司 | Method for purifying quinoline insoluble coal-series asphalt with high softening point and high softening point |
| CN109518230A (en) * | 2019-01-21 | 2019-03-26 | 中南大学 | A kind of encryption anode carbon block impregnating agent and preparation method thereof |
| CN111363577A (en) * | 2020-03-12 | 2020-07-03 | 中国科学院山西煤炭化学研究所 | Spinnable asphalt for coal-based general-grade asphalt carbon fibers and preparation method thereof |
| CN115197733A (en) * | 2022-06-29 | 2022-10-18 | 鞍钢化学科技有限公司 | Low-QI impregnant asphalt preparation system and process |
| CN115197733B (en) * | 2022-06-29 | 2024-03-15 | 鞍钢化学科技有限公司 | Low QI impregnant asphalt preparation system and process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103242880B (en) | 2014-11-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103242880B (en) | High-quality impregnant asphalt production process | |
| CN104650938B (en) | Needle coke, MCMB, the joint production process method of high-quality asphalt | |
| CN101787298B (en) | Coal art pitch purification method | |
| CN101508903B (en) | Process for continuously removing quinoline insoluble substances in coal tar pitch | |
| CN101475820A (en) | Purification method for coal pitch | |
| CN101824329A (en) | Novel process for eliminating quinoline insoluble substances in coal tar medium temperature pitch | |
| CN101531909A (en) | Continuous sedimentation process for production of needle coke | |
| CN101928583A (en) | Method for purifying soft asphalt | |
| CN103275754B (en) | Method for separating liquefied heavy oil and asphalt substrate from direct coal liquefaction residues | |
| CN101993704A (en) | Method for removing quinoline insoluble substances in coal tar pitch | |
| CN101798515A (en) | Process for co-production of high-quality carbon black raw oil, refined asphalt and binder asphalt | |
| CN104789248A (en) | Method for preparing mesophase pitch by coal-tar pitch | |
| CN104479707B (en) | A kind of method for preparing needle coke | |
| CN102839008A (en) | Purification method for coal tar soft pitch | |
| CN105713635A (en) | Method for removing quinoline-insoluble substances in coal tar | |
| CN103710039A (en) | Technology for one-step production of maltha from coal tar | |
| CN208346102U (en) | The pretreatment of raw material solvent extraction system of needle coke industrialized production | |
| CN102533319B (en) | Method for removing basic nitrogen compounds in oils | |
| CN105612245B (en) | The manufacturing method of ashless coal | |
| CN104080893A (en) | Solvent separation method | |
| CN101220284B (en) | Method for producing electrode impregnation asphalt | |
| CN108893140A (en) | A method of branded oil system needle-shape coke raw material is produced by solvent separation and Extraction | |
| CN108395904B (en) | Raw material pretreatment solvent extraction system and method for needle coke industrial production | |
| CN110628447B (en) | Pretreatment early-stage process for coal-based needle coke raw material | |
| KR101584564B1 (en) | System and method for upgrading heavy oil using solvent deasphalting process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170717 Address after: 430083, Gate No. 2, Qingshan District, Hubei, Wuhan Patentee after: Wuhan iron and Steel Company Limited Address before: 430080 Wuhan, Hubei Friendship Road, No. 999, Wuchang Patentee before: Wuhan Iron & Steel (Group) Corp. |
|
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20141119 Termination date: 20180508 |