CN101928600A - Method for producing diesel oil or diesel oil blending component - Google Patents
Method for producing diesel oil or diesel oil blending component Download PDFInfo
- Publication number
- CN101928600A CN101928600A CN200910148611XA CN200910148611A CN101928600A CN 101928600 A CN101928600 A CN 101928600A CN 200910148611X A CN200910148611X A CN 200910148611XA CN 200910148611 A CN200910148611 A CN 200910148611A CN 101928600 A CN101928600 A CN 101928600A
- Authority
- CN
- China
- Prior art keywords
- oil
- diesel oil
- cut
- diesel
- accordance
- 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
Abstract
The invention discloses a method for producing diesel oil or a diesel oil blending component. The method comprises the following steps of: mixing Fischer-Tropsch synthetic oil and direct coal liquefaction oil to obtain mixed oil; and performing hydrofining and hydrogenation isocracking on the mixed oil and performing fractionation to obtain a diesel oil product or the diesel oil blending component. In the method provided by the invention, two types of oil prepared from coal can be transformed into clean diesel oil which is accordant with a European IV standard or the diesel oil blending component with a large cetane number. Compared with hydrogenation modification of the direct coal liquefaction oil, the method has the advantages of temperate reaction condition, low device investment cost and low operation cost.
Description
Technical field
The present invention relates to a kind of oil of producing by coal and produce the method for diesel oil or diesel oil blending component.More particularly, be by coal direct liquefaction oil and ICL for Indirect Coal Liquefaction oil in the presence of hydrogen, produce the method for diesel oil or diesel oil blending component.
Background technology
The high speed development of Chinese national economy continues vigorous to the demand of the energy, since China in 1993 becomes net import of oil state, the oil insufficiency of supply-demand enlarges year by year, the external interdependency of crude oil raises year by year, the external interdependency of crude oil was 43% in 2006, surpassed 46% in 2007, and estimated that the year two thousand twenty will reach 60%.The fluctuation of international petroleum market and variation will directly influence the safety of China's economy and even politics and stablize.Solve liquid fuel supply and demand problem by non-petroleum path synthetic liquid fuel, not only satisfy the requirement of national energy strategic security, and Sustainable development steady in a long-term has important promoter action to national economy.
In numerous substitute energy technology, the Fischer-Tropsch synthetic technology becomes the focus of various countries, each major oil companies' technological development.Fischer-Tropsch synthetic raw material sources are extensive, and coal, Sweet natural gas, associated gas, refinery's lighter hydrocarbons, poor residuum etc. all can be used as the raw materials for production of synthetic gas.Fischer-Tropsch synthesis has two technological lines of pyroprocess and low temperature process according to purpose product difference.Pyroprocess is mainly produced gasoline and various high added value chemical, and low temperature process is mainly produced heavy hydrocarbon.The liquid fuel combustion performance that adopts the Fischer-Tropsch synthetic technology to produce is good, and exhaust emission is little, is called as clean energy.The ICL for Indirect Coal Liquefaction technology is owing to have raw material and adapt to strong and advantage, the abroad successful example of existing commercial operation such as oil quality is good: Sasol company has about 7,400,000 tons three factories that synthesize oil products of annual output in South Africa; Shell company has the factory that produces about 540,000 tons synthetic oil products per year in Malaysia.Other oil companies such as ExxonMobil, Chevron, Topsoe, IFP etc. all research and develop energetically in the Fischer-Tropsch synthesis technical field.
CN1780899A discloses a kind of method by low temperature Fischer-Tropsch raw material production synthetic low sulphur diesel fuel.This method fractionates out diesel oil distillate with Fischer-Tropsch synthesis oil, and diesel oil distillate and the mixing of petroleum base diesel oil obtain diesel oil fuel.
US6858127 discloses a kind of method of producing intermediate oil.At least contain the C30+ hydro carbons of 40 weight % in the Fischer-Tropsch synthesis oil of being processed in this method, this raw material is carried out the hydroisomerizing cracking reaction, the reaction product fractionation obtains intermediate oil and hydrogenation tail oil, and hydrogenation tail oil carries out the hydroisomerizing cracking reaction.
US5378348 discloses a kind of method of being produced intermediate oil by Fischer-Tropsch wax.In this method the Fischer-Tropsch synthetic wax is divided into two cuts of weight (cut point is 260 ℃), the hydroisomerization processing is carried out in last running, and hydrotreatment and hydroisomerization are carried out in lighting end.Wherein isomerization catalyst is a noble metal catalyst.
US6787022 discloses a kind of method of being produced diesel oil by Fischer-Tropsch wax.With Fischer-Tropsch synthetic＞149 ℃ of cuts are raw material, this raw material at first carries out isomerization reaction at first reaction zone, reaction product enters second reaction zone and carries out catalytic dewaxing reaction then.Isomerization catalyst is the noble metal catalyst that is carried on the amorphous silicon aluminium, the spherical catalyst of dewaxing catalyst for being composited by isomerization catalyst and dewaxing catalyst.
Just having begun DCL/Direct coal liquefaction produced the liquid hydrocarbon product Study on Technology as far back as 1913 in Germany, and will make the skilled industryization of gasoline with the brown coal direct liquefaction in nineteen twenty-seven.Since the world oil crisis first time taking place in 1973, direct coal liquefaction technology is subjected to the attention of developed country, has developed many DCL/Direct coal liquefaction technologies in succession.
CN1896181A discloses the method that a kind of coal direct liquefaction oil is produced high hexadecane value diesel oil.Coal direct liquefaction oil can the production cetane value be higher than 45 diesel oil by hydrofining and hydro-upgrading.
Liquid hydrocarbon by the synthetic preparation of Fischer-Tropsch has the extremely low advantage of sulphur nitrogen content, and diesel cetane-number can reach more than 70～80, but its density is lower, generally is lower than 0.78g/cm
3, can not directly be used as derv fuel oil, can only use as blending component.DCL/Direct coal liquefaction is another approach of coal system oil, but the DCL/Direct coal liquefaction oil quality is very poor, and the diesel oil distillate cetane value is very low, generally is lower than 30, is difficult to produce high-quality diesel under the hydro-upgrading condition of routine.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of and produce the method that oil is produced diesel product or high hexadecane value diesel oil blending component with coal.
Method provided by the invention may further comprise the steps:
(1) mixes Fischer-Tropsch synthesis oil and coal direct liquefaction oil, obtain mixing oil;
(2) mixing oil and hydrogen enter the hydrofining reaction district after mixing, and contact with Hydrobon catalyst under the hydrofining condition, obtain hydrofined oil; The fractionation hydrofined oil obtains comprising the cut of diesel oil distillate I and tail oil cut I;
(3) tail oil cut I enters hydroisomerizing cracking reaction district, contacts with the hydroisomerizing cracking catalyst under the hydroisomerizing cracking conditions, obtains hydrocrackates; The fractionation hydrocrackates obtains comprising the cut of diesel oil distillate II and tail oil cut II;
(4) the tail oil cut II of step (3) gained loops back hydroisomerizing cracking reaction district and carries out the hydroisomerizing cracking reaction;
(5) Medium diesel oil cut I and diesel oil distillate II obtain diesel product or diesel oil blending component.
The blending ratio of described Fischer-Tropsch synthesis oil and coal direct liquefaction oil is 5: 95 (weight ratio)～95: 5 (weight ratio), and preferred blending ratio is 30: 70 (weight ratio)～70: 30 (weight ratio).
Coal direct liquefaction oil is the product oil that hydrogenation under reaction conditions obtains by coal and solvent.Described DCL/Direct coal liquefaction reaction conditions is 250～550 ℃ of temperature of reaction, hydrogen dividing potential drop 15～40MPa.The boiling range of coal direct liquefaction oil of the present invention is 50～500 ℃.
Described Fischer-Tropsch synthesis oil is the low temperature Fischer-Tropsch synthesis oil, and boiling range is 20～680 ℃.The low temperature Fischer-Tropsch synthesis oil be by hydrogen and carbon monoxide under the low temperature Fischer-Tropsch synthesis condition with the liquid hydrocarbon that obtains after fischer-tropsch synthetic catalyst contacts.Described low temperature Fischer-Tropsch synthesis condition is 160～250 ℃ of temperature of reaction, pressure 1.5～4.0MPa, air speed 300～3000h
-1, hydrogen/carbon monoxide mol ratio 1.5～2.5.Described fischer-tropsch synthetic catalyst is a Co based Fischer-Tropsch synthesis catalyst.
Mixing oil removes most of alkene, oxygen, colloid in hydrofining reactor, the polycyclic aromatic hydrocarbons fractional saturation.Described hydrofining condition is hydrogen dividing potential drop 2.0～15.0MPa, 250～400 ℃ of temperature of reaction, hydrogen to oil volume ratio 100～1000v/v, volume space velocity 0.5～10.0h
-1
Described Hydrobon catalyst is a kind of metal load type catalyst, and carrier is unformed aluminum oxide, and metal component is VIB or/and VIII family base metal, and wherein the group vib metal is Mo or/and W, and VIII family metal is that Co is or/and Ni.
The reactant flow in described hydrofining reaction district is separated through cooling off laggard promoting the circulation of qi liquid, capable of circulation time reaction zone of separating obtained hydrogen-rich gas, and separating obtained liquid stream enters separation column.The separation column cutting obtains naphtha fraction I, diesel oil distillate I and tail oil cut I, and wherein the cut point between naphtha fraction I and the diesel oil distillate I is 140 ℃～180 ℃, and the cut point between diesel oil distillate I and the tail oil cut I is 300 ℃～360 ℃.
The tail oil cut I of gained enters isomery and/or the cracking reaction that hydroisomerizing cracking reaction district carries out hydro carbons.Described hydroisomerizing cracking conditions is hydrogen dividing potential drop 2.0～15.0MPa, 300～450 ℃ of temperature of reaction, hydrogen to oil volume ratio 100～1500v/v, volume space velocity 0.5～5.0h
-1
Noble metal catalyst or non-precious metal catalyst that described hydroisomerizing cracking catalyst is the amorphous silicon aluminium load, the metal component of non-precious metal catalyst is that VIB is or/and VIII family base metal, wherein the group vib metal is Mo or/and W, and VIII family metal is that Co is or/and Ni; The metal component of noble metal catalyst is that Pt is or/and Pd.
The reactant flow in described hydroisomerizing cracking reaction district is separated through cooling off laggard promoting the circulation of qi liquid, capable of circulation time reaction zone of separating obtained hydrogen-rich gas, and separating obtained liquid stream enters separation column.The separation column cutting obtains naphtha fraction II, diesel oil distillate II and tail oil cut II, and wherein the cut point between naphtha fraction II and the diesel oil distillate II is 140 ℃～180 ℃, and the cut point between diesel oil distillate II and the tail oil cut II is 310 ℃～370 ℃.
Advantage of the present invention:
(1) Fischer-Tropsch synthesis oil upgrading gained diesel oil has the advantages that density is low, cetane value is high, and density generally is lower than 0.78g/cm
3, cetane value generally can reach more than 75; Coal direct liquefaction oil upgrading gained diesel oil has density height, characteristics that cetane value is low, and density generally is higher than 0.86g/cm
3, cetane value generally is lower than 30.The upgrading diesel oil of the two all can't directly directly use as commercial Dissel oil, and by method provided by the invention, Fischer-Tropsch synthesis oil and coal direct liquefaction oil are by the mixed hydrogenation upgrading, and its diesel oil distillate can directly use as commercial Dissel oil.
(2) with respect to the hydro-upgrading of coal direct liquefaction oil, the reaction conditions of Fischer-Tropsch synthesis oil and coal direct liquefaction oil mixed hydrogenation upgrading comparatively relaxes, and has reduced the device process cost.
Description of drawings
Accompanying drawing is the schematic flow sheet of the method for production diesel oil provided by the invention or diesel oil blending component.
Embodiment
Below in conjunction with accompanying drawing method provided by the present invention is given further instruction, but therefore the present invention is not subjected to any restriction.
Technological principle schematic flow sheet of the present invention is seen accompanying drawing.Flow process is described below: the mixture flow 1 of mixing oil and hydrogen enters hydrofining reactor A reaction, and the effluent 2 of hydrofining reactor A enters hydrotreatment separation column B to carry out fractionation and be cut into naphtha fraction 3, diesel oil distillate 4 and tail oil cut 5; Tail oil cut 5 mixes the back and enters hydroisomerizing cracking case C as logistics 6 with unconverted tail oil cut 10 from separation column D, mend hydrogen 11 to regulate the hydrogen-oil ratio in hydroisomerizing cracking reaction district at hydroisomerizing cracking case inlet.Hydrocracking and/or isomerization reaction take place under the effect of hydroisomerizing cracking catalyst, reaction product is that logistics 7 enters separation column D cutting and obtains naphtha fraction 8, diesel oil distillate 9 and tail oil cut 10, unconverted heavy ends be tail oil cut 10 loop back hydroisomerizing cracking case C proceed the reaction, finally realize the full conversion of heavy ends.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
The character of testing used Fischer-Tropsch synthesis oil and coal direct liquefaction oil sees Table 1, and the two obtains mixing oil after mixing according to a certain percentage.
The trade names of testing used Hydrobon catalyst are RTF-1, and the trade names of hydroisomerizing cracking catalyst are RCF-1.Be the Chang Ling catalyst plant production of catalyzer branch office of China Petrochemical Industry.
Adopt fixed bed hydrogenation reactor, double-reactor operation, wherein anti-Hydrobon catalyst RTF-1, the catalyzer loading amount 100ml of loading; Two anti-filling hydroisomerizing cracking catalyst RCF-1, catalyzer loading amount 60ml.
Fischer-Tropsch synthesis oil and coal direct liquefaction oil obtain stock oil A according to 30: 70 mixed, and its character sees Table 2, carry out the hydro-upgrading of mixing oil according to method provided by the invention, and the inlet amount of mixing oil is 123g/h.
Hydrofining reaction district operational condition is: 320 ℃ of temperature, hydrogen dividing potential drop 6.4MPa, hydrogen to oil volume ratio 450.
Hydroisomerizing cracking reaction district operational condition is: 365 ℃ of temperature, hydrogen dividing potential drop 6.4MPa, hydrogen to oil volume ratio 800.
The temperature range of separation column B cutting distillate is: naphtha fraction I is＜150 ℃, and diesel oil distillate I is 150～340 ℃, and tail oil cut I is＞340 ℃.
The temperature range of separation column D cutting distillate is: naphtha fraction II is＜150 ℃, and diesel oil distillate II is 150～370 ℃, and tail oil cut II is＞370 ℃.
The diesel oil distillate I and the diesel oil distillate II that mix separation column B and separation column D, the diesel oil 1 that obtains, its character sees Table 3.
Fischer-Tropsch synthesis oil and coal direct liquefaction oil obtain stock oil B according to 50: 50 mixed, and its character sees Table 2, carry out the hydro-upgrading of mixing oil according to method provided by the invention, and the inlet amount of mixing oil is 138g/h.
Hydrofining reaction district operational condition is: 315 ℃ of temperature, hydrogen dividing potential drop 6.4MPa, hydrogen to oil volume ratio 400.
Hydroisomerizing cracking reaction district operational condition is: 365 ℃ of temperature, hydrogen dividing potential drop 6.4MPa, hydrogen to oil volume ratio 800.
The temperature range of separation column B cutting distillate is: naphtha fraction I is＜150 ℃, and diesel oil distillate I is 150～330 ℃, and tail oil cut I is＞330 ℃.
The temperature range of separation column D cutting distillate is: naphtha fraction II is＜150 ℃, and diesel oil distillate II is 150～370 ℃, and tail oil cut II is＞370 ℃.
Mix diesel oil distillate I and the diesel oil distillate II of separation column B and separation column D, the character of the diesel oil 2 that obtains sees Table 3.
Fischer-Tropsch synthesis oil and coal direct liquefaction oil obtain stock oil C according to 80: 20 mixed, and its character sees Table 2, carry out the hydro-upgrading of mixing oil according to method provided by the invention, and the inlet amount of mixing oil is 150g/h.
Hydrofining reaction district operational condition is: 310 ℃ of temperature, hydrogen dividing potential drop 6.0MPa, hydrogen to oil volume ratio 400.
Hydroisomerizing cracking reaction district operational condition is: 365 ℃ of temperature, hydrogen dividing potential drop 6.0MPa, hydrogen to oil volume ratio 800.
The temperature range of separation column B cutting distillate is: naphtha fraction I is＜150 ℃, and diesel oil distillate I is 150～320 ℃, and tail oil cut I is＞320 ℃.
The temperature range of separation column D cutting distillate is: naphtha fraction II is＜150 ℃, and diesel oil distillate II is 150～370 ℃, and tail oil cut II is＞370 ℃.
Mix diesel oil distillate I and the diesel oil distillate II of separation column B and separation column D, the character of the diesel oil 3 that obtains sees Table 3.
By embodiment in the table 31 and embodiment 2 data as can be seen, by the diesel oil that the method for the invention obtains, its index meets European IV derv fuel oil standard.By the data of embodiment 3 as can be seen, when the Fischer-Tropsch synthesis oil blending ratio is higher in the raw material, the density of product diesel oil is lower, can not meet European IV derv fuel oil standard, all the other indexs can reach European IV derv fuel oil standard, but the products obtained therefrom diesel-fuel cetane number is very high, is fine high hexadecane value diesel oil blending component.
Table 1 Fischer-Tropsch synthesis oil and DCL/Direct coal liquefaction oil nature
| Fischer-Tropsch synthesis oil | Coal direct liquefaction oil | |
| Density (20 ℃), g/cm 3 | 0.7910 | 0.9869 |
| Viscosity (20 ℃), mm 2/s | / | 42.21 |
| Condensation point, ℃ | / | 12 |
| Carbon residue, weight % | / | 13.2 |
| The bromine valency, gBr/100g | 11.3 | 20.8 |
| Polycyclic aromatic hydrocarbons, weight % | 0 | 31.0 |
| Sulphur content, μ g/g | ＜5 | 396 |
| Oxygen level, weight % | 1.01 | 1.29 |
| Boiling range, |
||
| 5％ | 101 | 248 |
| 50％ | 372 | 326 |
| 90％ | 555 | 420 |
| 95％ | 616 | 453 |
Table 2 mixing oil character
| Mixing oil A | Mixing oil B | Mixing oil C | |
| Density (20 ℃), g/cm 3 | 0.9282 | 0.8890 | 0.8301 |
| Carbon residue, weight % | 9.36 | 6.82 | 2.70 |
| The bromine valency, gBr/100g | 18.63 | 16.38 | 13.25 |
| Oxygen level, weight % | 1.21 | 1.15 | 1.07 |
| Boiling range, |
|||
| 5％ | 195 | 169 | 135 |
| 50％ | 341 | 351 | 365 |
| 90％ | 480 | 489 | 516 |
| 95％ | 532 | 543 | 597 |
Table 3 diesel oil character
Claims (11)
1. method of producing diesel oil or diesel oil blending component comprises:
(1) mixes Fischer-Tropsch synthesis oil and coal direct liquefaction oil, obtain mixing oil;
(2) mixing oil and hydrogen enter the hydrofining reaction district after mixing, and contact with Hydrobon catalyst under the hydrofining condition, obtain hydrofined oil; The fractionation hydrofined oil obtains comprising the cut of diesel oil distillate I and tail oil cut I;
(3) tail oil cut I enters hydroisomerizing cracking reaction district, contacts with the hydroisomerizing cracking catalyst under the hydroisomerizing cracking conditions, obtains hydrocrackates; The fractionation hydrocrackates obtains comprising the cut of diesel oil distillate II and tail oil cut II;
(4) the tail oil cut II of step (3) gained loops back hydroisomerizing cracking reaction district and carries out the hydroisomerizing cracking reaction;
(5) Medium diesel oil cut I and diesel oil distillate II obtain diesel product or diesel oil blending component.
2. in accordance with the method for claim 1, the blending ratio that it is characterized in that described Fischer-Tropsch synthesis oil and coal direct liquefaction oil is 5: 95 (weight ratio)～95: 5 (weight ratio).
3. in accordance with the method for claim 1, the blending ratio that it is characterized in that described Fischer-Tropsch synthesis oil and coal direct liquefaction oil is 30: 70 (weight ratio)～70: 30 (weight ratio).
4. in accordance with the method for claim 1, the boiling range that it is characterized in that described coal direct liquefaction oil is 50～500 ℃.
5. in accordance with the method for claim 1, it is characterized in that Fischer-Tropsch synthesis oil is the low temperature Fischer-Tropsch synthesis oil, boiling range is 20～680 ℃.
6. in accordance with the method for claim 1, it is characterized in that described hydrofining condition is hydrogen dividing potential drop 2.0～15.0MPa, 250～400 ℃ of temperature of reaction, hydrogen to oil volume ratio 100～1000v/v, volume space velocity 0.5～10.0h
-1
7. in accordance with the method for claim 1, it is characterized in that described hydroisomerizing cracking conditions is hydrogen dividing potential drop 2.0～15.0MPa, 300～450 ℃ of temperature of reaction, hydrogen to oil volume ratio 100～1500v/v, volume space velocity 0.5～5.0h
-1
8. in accordance with the method for claim 1, it is characterized in that described Hydrobon catalyst is a kind of metal load type catalyst, carrier is unformed aluminum oxide, and metal component is that VIB is or/and VIII family base metal, wherein the group vib metal is Mo or/and W, and VIII family metal is that Co is or/and Ni.
9. in accordance with the method for claim 1, it is characterized in that noble metal catalyst or non-precious metal catalyst that described hydroisomerizing cracking catalyst is the amorphous silicon aluminium load, the metal component of non-precious metal catalyst is that VIB is or/and VIII family base metal, wherein the group vib metal is Mo or/and W, and VIII family metal is that Co is or/and Ni; The metal component of noble metal catalyst is that Pt is or/and Pd.
10. in accordance with the method for claim 1, it is characterized in that diesel oil distillate I and the cut point between the tail oil cut I in the described step (2) are 300 ℃～360 ℃.
11. in accordance with the method for claim 1, it is characterized in that diesel oil distillate II and the cut point between the tail oil cut II in the described step (3) are 310 ℃～370 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200910148611 CN101928600B (en) | 2009-06-25 | 2009-06-25 | Method for producing diesel oil or diesel oil blending component |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200910148611 CN101928600B (en) | 2009-06-25 | 2009-06-25 | Method for producing diesel oil or diesel oil blending component |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101928600A true CN101928600A (en) | 2010-12-29 |
| CN101928600B CN101928600B (en) | 2013-06-05 |
Family
ID=43368039
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200910148611 Active CN101928600B (en) | 2009-06-25 | 2009-06-25 | Method for producing diesel oil or diesel oil blending component |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101928600B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102911729A (en) * | 2011-08-01 | 2013-02-06 | 中国石油化工股份有限公司 | Method for producing diesel oil from Fischer-Tropsch synthetic oil |
| CN102911722A (en) * | 2011-08-01 | 2013-02-06 | 中国石油化工股份有限公司 | Hydrogenation quality-improving method for Fischer-Tropsch synthetic oil |
| CN103131468A (en) * | 2013-02-06 | 2013-06-05 | 神华集团有限责任公司 | Hydrofining and/or hydroisomerizing cracking system and process for low-temperature Fischer-Tropsch synthetic oil |
| CN105925305A (en) * | 2016-04-20 | 2016-09-07 | 神华集团有限责任公司 | Diesel oil and preparation method thereof |
| WO2017181813A1 (en) * | 2016-04-18 | 2017-10-26 | 武汉凯迪工程技术研究总院有限公司 | Method and equipment thereof for producing high-quality diesel using low-temperature fischer-tropsch synthetic oil and low-grade oil feedstock |
| CN110003946A (en) * | 2019-05-17 | 2019-07-12 | 国家能源投资集团有限责任公司 | The system and method for indirect liquefaction oil and direct liquefaction oil reconciliation production petrol and diesel oil |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5378348A (en) * | 1993-07-22 | 1995-01-03 | Exxon Research And Engineering Company | Distillate fuel production from Fischer-Tropsch wax |
| US20040074810A1 (en) * | 2001-03-05 | 2004-04-22 | Arend Hoek | Process for the preparation of middle distillates |
| CN1896181A (en) * | 2005-07-15 | 2007-01-17 | 中国石油化工股份有限公司 | Production of high-bioctyl-value diesel oil by coal liquification |
| WO2008083601A1 (en) * | 2006-12-30 | 2008-07-17 | Accelergy Shanghai R & D Center Co., Ltd. | An integrated coal liquefaction process |
-
2009
- 2009-06-25 CN CN 200910148611 patent/CN101928600B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5378348A (en) * | 1993-07-22 | 1995-01-03 | Exxon Research And Engineering Company | Distillate fuel production from Fischer-Tropsch wax |
| US20040074810A1 (en) * | 2001-03-05 | 2004-04-22 | Arend Hoek | Process for the preparation of middle distillates |
| CN1896181A (en) * | 2005-07-15 | 2007-01-17 | 中国石油化工股份有限公司 | Production of high-bioctyl-value diesel oil by coal liquification |
| WO2008083601A1 (en) * | 2006-12-30 | 2008-07-17 | Accelergy Shanghai R & D Center Co., Ltd. | An integrated coal liquefaction process |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102911729A (en) * | 2011-08-01 | 2013-02-06 | 中国石油化工股份有限公司 | Method for producing diesel oil from Fischer-Tropsch synthetic oil |
| CN102911722A (en) * | 2011-08-01 | 2013-02-06 | 中国石油化工股份有限公司 | Hydrogenation quality-improving method for Fischer-Tropsch synthetic oil |
| CN102911722B (en) * | 2011-08-01 | 2014-10-29 | 中国石油化工股份有限公司 | Hydrogenation quality-improving method for Fischer-Tropsch synthetic oil |
| CN102911729B (en) * | 2011-08-01 | 2014-12-03 | 中国石油化工股份有限公司 | Method for producing diesel oil from Fischer-Tropsch synthetic oil |
| CN103131468A (en) * | 2013-02-06 | 2013-06-05 | 神华集团有限责任公司 | Hydrofining and/or hydroisomerizing cracking system and process for low-temperature Fischer-Tropsch synthetic oil |
| WO2017181813A1 (en) * | 2016-04-18 | 2017-10-26 | 武汉凯迪工程技术研究总院有限公司 | Method and equipment thereof for producing high-quality diesel using low-temperature fischer-tropsch synthetic oil and low-grade oil feedstock |
| CN105925305A (en) * | 2016-04-20 | 2016-09-07 | 神华集团有限责任公司 | Diesel oil and preparation method thereof |
| CN110003946A (en) * | 2019-05-17 | 2019-07-12 | 国家能源投资集团有限责任公司 | The system and method for indirect liquefaction oil and direct liquefaction oil reconciliation production petrol and diesel oil |
| CN110003946B (en) * | 2019-05-17 | 2021-07-30 | 国家能源投资集团有限责任公司 | System and method for producing gasoline and diesel oil by blending indirect liquefied oil and direct liquefied oil |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101928600B (en) | 2013-06-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101928599B (en) | Method for producing jet fuel or jet fuel blending component | |
| CN111117701B (en) | Hydrogenation method for maximum production of heavy naphtha and jet fuel components | |
| JP6501897B2 (en) | Process for hydrotreating low temperature Fischer-Tropsch synthesis product | |
| EP2964592B1 (en) | Process of catalytic production of diesel fuel | |
| CN101928600B (en) | Method for producing diesel oil or diesel oil blending component | |
| CN101210198A (en) | Hydrogenation method for producing high grade diesel oil and high grade reforming raw material | |
| RU2577547C2 (en) | Fischer-tropsch process improvement for production of hydrocarbon fuel in conditions of gas-to-liquids technology | |
| JP2007511634A (en) | Method for improving the quality of Fischer-Tropsch products | |
| JP2018510934A (en) | Diesel and jet fuel production systems and methods using Fischer-Tropsch synthetic oil | |
| GB2385861A (en) | Removal of carbon oxides from Fischer-Tropsch products prior to hydroprocessing | |
| CN104004541B (en) | A kind of preparation method of coal-based high arene underwater content stock oil | |
| CN101230291B (en) | Low consumption energy method for processing fischer-tropsch synthesis | |
| CN102061191A (en) | Method for producing solvent oil or blended components thereof | |
| CN100395315C (en) | Hydrogenation purifying combined process for Fischer-Tropsch synthetic substance | |
| US20150322351A1 (en) | Integrated gas-to-liquid condensate process | |
| CN100389169C (en) | Production of high-bioctyl-value diesel oil by coal liquification | |
| CN109988609B (en) | Flexible shale oil hydrocracking process | |
| US9587183B2 (en) | Integrated gas-to-liquid condensate process and apparatus | |
| WO2023150001A1 (en) | Production of sustainable aviation fuel from co2 and low-carbon hydrogen | |
| CN100419044C (en) | Production of large-specific-weight aircraft liquid petroleum oil at maximum from coal liquefied oil | |
| US20150337212A1 (en) | Integrated gas-to-liquids condensate process | |
| CN111117696B (en) | Hydrocracking method | |
| CN105295991B (en) | It is a kind of to improve the method that Fischer-Tropsch wax is hydrocracked midbarrel oil yield | |
| CN102041080A (en) | Integrated method for hydrocracking and producing ethylene cracking material | |
| CN106398762A (en) | Method for producing middle distillate oil through hydrogenation of Fischer-Tropsch synthesis oil |
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 |