CN1896189A - Production of large-specific-weight aircraft liquid petroleum oil at maximum from coal liquefied oil - Google Patents
Production of large-specific-weight aircraft liquid petroleum oil at maximum from coal liquefied oil Download PDFInfo
- Publication number
- CN1896189A CN1896189A CN 200510083900 CN200510083900A CN1896189A CN 1896189 A CN1896189 A CN 1896189A CN 200510083900 CN200510083900 CN 200510083900 CN 200510083900 A CN200510083900 A CN 200510083900A CN 1896189 A CN1896189 A CN 1896189A
- Authority
- CN
- China
- Prior art keywords
- reactor
- hydrogenation
- hydrogen
- catalyst
- reaction
- 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
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Production of large-specific weight aviation kerosene from coal liquefied oil at maximum is carried out by entering coal liquefied oil into protective reactor, contacting it with hydrogen and protective agent, entering reactant of protective reactor into stabilized hydrogenation main reactor, contacting with hydrogen and hydrogenation stabilized catalyst, separating for reactant of stabilized hydrogenation main reactor to obtain intermediate distillate, entering it into hydrogenation qualified reactor, contacting with hydrogen, hydrogenation refined catalyst and hydrogenation qualified catalyst and separating from reactant of hydrogenation qualified reactor to obtain the final product. The recovery rate of aviation kerosene can reach to 45% and its specific weight is >0.84g/cm3.
Description
Technical field
The present invention relates to the method that a kind of liquid hydrocarbon that coal destruction hydrogenation is obtained carries out hydrotreatment.More particularly, be a kind of method of producing aviation kerosene from liquefied coal coil.
Background technology
Coal and oil are main primary energy source.China is the country of a rich coal resources, has verified coal reserves and has reached more than 1,000,000,000,000 ton, and annual production reaches 1,000,000,000 tons.The China's oil resource is deficient relatively, has only a large amount of imports could solve huge imbalance between supply and demand.On the other hand, strict gradually environmental regulation requires to use clean fuel, forces the primary energy source structure to be adjusted, and the proportion of coal will descend, and the proportion of oil will rise.With the coal is that alternative materials production oil fuel is to realize one of basic self-supporting realistic approach of China's oil product, also is the means that coal changed into clear energy sources, meets the national sustainable development strategy.
The gelatin liquefaction synthetic oil is two kinds of direct liquefaction and indirect liquefactions.Coal direct liquefaction oil contains impurity such as N, O, S, and because it is formed based on the ring-type hydro carbons, character is relatively poor during as the coal diesel oil distillate, need further carry out hydrotreatment, to improve the quality of products, obtains light Fuel products such as qualified vapour, coal, diesel oil.
Big proportion aviation kerosene is called rocket engine fuel again No. 6, because its density is big, the calorific value of unit volume can improve the voyage after aircraft once refuels than common rocket engine fuel height during as aviation fuel.
USP4332666 has announced a kind of method of producing diesel oil, aviation fuel or oil fuel from liquefied coal coil, this method is carried out hydrogenation with the cut that is fit to do hydrogen supply agent in the liquefied coal coil, extract naphthenic hydrocarbon in the hydrogenation products then out as diesel oil, aviation fuel or oil fuel, remaining as the unitary hydrogen supply agent of gelatin liquefaction.But the aviation fuel yield of being produced by this method is lower, and smoke point is lower.
USP4569749 has announced a kind of method of producing light oil fuel from coal.This method comprises hydrofining two portions of liquidation of coal and liquefaction oil lighter fraction, and the last running of liquefaction oil loops back the gelatin liquefaction unit, and hydrotreatment is carried out in remaining lighting end, middle runnings.Doing of unifining process charging is not more than 310 ℃, and foreign matter contents such as the sulphur of product, nitrogen are low, and color is good.Product is based on naphtha fraction and middle runnings, and naphtha fraction is good reformer feed, but intermediate oil is second-rate.
EP0321713 has announced a kind of method from the big proportion aviation kerosene of gelatin liquefaction heavy oil production.In this method, raw material is the last running of liquefied coal coil, and it 50% distillates o'clock about 450 ℃.Raw material at first carries out hydrocracking, and the lighting end of isocrackate enters hydrotreating reactor after cooling, carry out hydrodenitrification, and product enters the 3rd hydrogenator again and carries out the mild hydrogenation processing, makes aromatic hydrocarbons saturated.The characteristics of this method are that with the heavy liquefied coal coil be raw material, carry out hydrocracking earlier, carry out hydrofining then, aromatic hydrocarbons is saturated, to produce big proportion aviation kerosene.Owing to be to be the raw material production kerosene(oil)fraction with the mink cell focus, its hydrogen-consuming volume must be higher.In addition, because foreign matter contents such as liquefied coal coil nitrogen are higher, raw material hydrofining is not handled again before the hydrocracking, the easy inactivation of hydrocracking catalyst, for guaranteeing that activity of such catalysts is stable, hydrocracking catalyst need adopt active more weak catalyzer, for guaranteeing certain transformation efficiency, need operation at high temperature, so its running period will be than the weak point of conventional hydroeracking unit.
It is a kind of to be rich in the method for two rings, the big proportion aviation kerosene of polycyclic aromatic hydrocarbons raw material production that GB2234518 provides.The raw material that is rich in aromatic hydrocarbons can come catalytic cracking light cycle oil, furnace fuel oil, liquefied coal coil or shale wet goods.Stock oil with enter first hydrogenator after hydrogen mixes and carry out hydrogenating desulfurization, denitrification reaction, second reactor adopts fluorine-containing noble metal catalyst to take off aromatic hydrocarbons, to improve quality product.For guaranteeing the activity stabilized of two anti-noble metal catalysts, otherwise one anti-, two need are established separator with the H that generates
2S, NH
3Separate.
The production aviation kerosene yield that has in the prior art is lower, and it is lower to produce aviation kerosene proportion.
Summary of the invention
The objective of the invention is on the prior art basis, to provide a kind of method of producing big proportion aviation kerosene from the liquefied coal coil maximum.
Method provided by the invention comprises:
Liquefied coal coil is introduced into guard reactor; contact with hydrogen, protective material; the reaction effluent of guard reactor enters the stable hydrogenation main reactor; contact with hydrogen, stabilized hydrogenation catalyzer; the middle cut that the reaction effluent of stable hydrogenation main reactor obtains through separation enters hydrogenation upgrading reactor; contact with hydrogen, Hydrobon catalyst, hydrogenation upgrading catalyzer, the reaction effluent of hydrogenation upgrading reactor obtains aviation kerosene through separation.
Method provided by the invention is raw material with the liquefied coal coil, and maximum is produced qualified big proportion aviation kerosene, serves as to calculate benchmark with the liquefied coal coil raw material, and the yield of aviation kerosene is up to 45 heavy %, and the proportion of aviation kerosene is greater than 0.84g/cm
3
Description of drawings
Accompanying drawing is the method synoptic diagram that maximum provided by the invention is produced qualified big proportion aviation fuel.
Embodiment
The invention provides a kind of method of producing qualified big proportion aviation fuel from the liquefied coal coil maximum.This method comprises stable hydrogenation and two steps of hydrogenation upgrading.
Step 1: stable hydrogenation
The purpose of stable hydrogenation is impurity such as the oxygen that removes liquefied coal coil, nitrogen, sulphur, and saturation of olefins improves its stability, for follow-up hydrogenation upgrading process is supplied raw materials, and provides hydrogen supply dissolvent for the gelatin liquefaction unit.
Stable hydrogenation provided by the invention is the off-line stable hydrogenation, promptly is independent of outside the gelatin liquefaction part, with gelatin liquefaction partial common hydrogen-feeding system, independently hydrogen source and hydrogen gas circulating system is not arranged.The advantage of off-line stable hydrogenation is not to be subjected to the influence of gelatin liquefaction part shutting down, avoids CO in the upstream gelatin liquefaction part gas phase
xEnter the stable hydrogenation device reaction and generate CH
4And the meaningless hydrogen that causes consumption has also reduced in the liquefied coal coil water vapor to greatest extent to the influence of stable hydrogenation catalyzer.
In the stable hydrogenation process, deoxidation, desulfurization and olefin saturation are all carried out easily, and the hydrodenitrification reaction is relatively difficult.Therefore, how the nitrogen content in the liquefied coal coil is removed to the main task that lower level just becomes stable hydrogenation.The catalyzer that the stable hydrogenation process is adopted among the present invention is the stabilized hydrogenation catalyzer with high hydrodenitrogenationactivity activity, can nitrogen be removed under relatively than the demulcent condition level of requirement.
Stabilized hydrogenation catalyzer of the present invention is a carrier with unformed aluminum oxide or sial, loaded metal component on it, metal component is VIB or VIII family non-precious metal catalyst or their combination, and wherein the group vib metal is selected from Mo or/and W, and VIII family metal is selected from Co or/and Ni.
Before the stable hydrogenation reactor, establish guard reactor among the present invention.The effect of guard reactor is solid particulate and the metal impurities that removes in the raw material, guarantees the activity stabilized of Primary Catalysts.
Load protective material in the guard reactor, protective material is VIB or VIII family non-precious metal catalyst or their combination that loads on unformed aluminum oxide or the silica-alumina supports, and wherein the group vib metal is selected from Mo or/and W, and VIII family metal is selected from Co or/and Ni.This type of protective material has bigger pore volume and specific surface area.
Guard reactor adopts the upflowing operation, and feeding manner is that reactant flow enters from the guard reactor bottom, and reaction product is from the reactor head laggard stable hydrogenation reactor that comes out.Adopt the upflowing operating method, the guard reactor bed becomes fluffy, can effectively avoid the deposition of tiny solid particulate matter at reactor inlet, slows down pressure reduction and occurs, and prolongs on-stream time.
Among the present invention, the volume of guard reactor is 5%～30% of a stable hydrogenation main reactor.
The reaction conditions of stable hydrogenation guard reactor provided by the invention is: hydrogen dividing potential drop 3.0～30.0MPa; 220～400 ℃ of temperature of reaction; Liquid hourly space velocity 0.2～20h
-1, hydrogen-oil ratio 200～2500v/v.
The reaction conditions of stable hydrogenation main reactor provided by the invention is: hydrogen dividing potential drop 3.0～30.0MPa; 270～450 ℃ of temperature of reaction; Liquid hourly space velocity 0.1～10h
-1, hydrogen-oil ratio 300～2800v/v.
Step 2: hydrogenation upgrading
Hydrogenation upgrading process can be an online mode with respect to the stable hydrogenation process, also can be offline mode.The difference of dual mode is a whether common recycle hydrogen system of stable hydrogenation and hydrogenation upgrading.Below describe, but therefore do not limit the present invention by offline mode.
The raw material of step 2 hydrogenation upgrading is the middle cut behind the stable hydrogenation, and the purpose of this step is further to improve the quality of liquefied coal coil, obtains the proper fuel product.
Among the present invention, hydrogenation upgrading process adopts two kinds of catalyzer.Two kinds of catalyzer can be seated in the reactor, also can be seated in two reactors.
In the time of in being seated in a reactor, top filling Hydrobon catalyst, bottom filling hydrogenation upgrading catalyzer, the reaction conditions of this reactor is: hydrogen dividing potential drop 3.0～30.0MPa; 270～450 ℃ of temperature of reaction; Liquid hourly space velocity 0.1～10h
-1, hydrogen-oil ratio 500～3000v/v.
In the time of in being seated in two reactors, first reactor charge Hydrobon catalyst, second reactor charge hydrogenation upgrading catalyzer, the volume ratio of first reactor catalyst and second reactor catalyst is 1: 1～10: 1, and the reaction conditions of first reactor is: hydrogen dividing potential drop 3.0～30.0MPa; 270～450 ℃ of temperature of reaction; Liquid hourly space velocity 0.1～10h
-1, hydrogen-oil ratio 500～3000v/v; The reaction conditions of second reactor is: hydrogen dividing potential drop 3.0～30.0MPa; 280～450 ℃ of temperature of reaction; Liquid hourly space velocity 0.1～20h
-1, hydrogen-oil ratio 500～3000v/v.
Hydrobon catalyst in the step 2 is a carrier with unformed aluminum oxide or sial, loaded metal component on it, metal component is VIB or VIII family non-precious metal catalyst or their combination, and wherein the group vib metal is selected from Mo or/and W, and VIII family metal is selected from Co or/and Ni.
Hydrogenation upgrading catalyzer in the step 2 is with the carrier that is combined as of unformed aluminum oxide or sial or they, loaded metal component on it, metal component is VIB or VIII family non-precious metal catalyst or their combination, and wherein the group vib metal is selected from Mo or/and W, and VIII family metal is selected from Co or/and Ni.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed, but does not therefore limit the present invention.
Accompanying drawing is the method synoptic diagram that maximum provided by the invention is produced qualified big proportion aviation fuel, has omitted the equipment of many necessity among the figure, as pump, air cooler and valve etc.
Flow process is described in detail as follows:
Liquefied coal coil after the filtration is after pipeline 34 enters pump 2; mix with new hydrogen from pipeline 1 and heat after together enter guard reactor 3 bottoms, the reaction mass that comes out in the guard reactor top enters stable hydrogenation reactor 5 through pipeline 4 with the circulating hydrogen from circulating hydrogen compressor 13 and reacts.The reaction product of coming out in stable hydrogenation reactor 5 bottoms enters high-pressure separator 7 through pipeline 6, after gas-liquid separation, the gas at high-pressure separator 7 tops is delivered to the reactive system recycle by recycle compressor 13, and the liquid of high-pressure separator bottom enters light pressure separator 10 through pipeline 9 and proceeds gas-oil separation.The gas on light pressure separator 10 tops is drawn through pipeline 12, the liquid stream of bottom then enters separation column 35 through pipeline 11 to carry out cut and cuts apart, gas, lighting end, tail oil cut are drawn through pipeline 14,15,16 respectively, and middle cut is then drawn raw material as the upgrading of step 2 hydrogenation through pipeline 17.
The middle cut of separation column 35 successively through pipeline 17, pump, pipeline 18 with enter hydrogenation upgrading first reactor 19 tops jointly after hydrogen from pipeline 1 mixes, the reactant flow of coming out from first reactor, 19 bottoms need not separated directly and entered second reactor head through pipeline 20, and the reaction product that second reactor comes out enters high-pressure separator 23 through pipeline 22 and carries out gas-oil separation.High-pressure separator 23 top gas are circulated back to reactor 19, reactor 21 respectively through recycle compressor 25, and the liquid stream of high-pressure separator 23 bottoms enters light pressure separator 24 through pipeline 27, carries out further gas-oil separation.The gas on light pressure separator 24 tops is drawn through pipeline 29, and the liquid stream of bottom then enters separation column 30 through pipeline 28.Separation column 30 top logistics are naphtha fraction, its sulphur, nitrogen content are low, virtue is dived high, drawing through pipeline 32 can be directly as the fine reformer feed, the separation column bottoms is a kerosene(oil)fraction, character such as its smoke point, flash-point, freezing point, viscosity satisfy the index request of No. 6 aviation kerosenes, draw through pipeline 33.
Method provided by the invention is raw material with the liquefied coal coil, and maximum is produced qualified big proportion aviation kerosene, serves as to calculate benchmark with the liquefied coal coil raw material, and the yield of aviation kerosene is up to 45 heavy %, and the proportion of aviation kerosene is greater than 0.84g/cm
3
The following examples will give further instruction to present method, but therefore not limit present method.
Liquefied coal coil character used among the embodiment is listed in table 1.The used Hydrobon catalyst of used stabilized hydrogenation catalyzer, the hydrogenation upgrading of protective material, stable hydrogenation, the trade names of hydrogenation upgrading catalyzer are respectively RG10-A/B, RJW-2, RN-10, RIC-1, produce by Sinopec Chang Ling catalyst plant.Test is carried out on medium-sized fixed bed hydrogenation device.The volume of guard reactor is 20% of a stable hydrogenation main reactor; used Hydrobon catalyst, the hydrogenation upgrading catalyzer of hydrogenation upgrading is seated in respectively in two reactors; first reactor charge Hydrobon catalyst; second reactor charge hydrogenation upgrading catalyzer, the volume ratio of first reactor catalyst and second reactor catalyst is 1: 1.
Embodiment
The reaction conditions of stable hydrogenation step, reaction product character are listed in table 2～3 respectively.Table 4～5 are respectively stock oil character, the reaction conditions of hydrogenation upgrading step, the tabulation of reaction product character.As can be seen from Table 1, nitrogen, the oxygen level height of liquefied coal coil before the stable hydrogenation, the bromine valency is higher.The data of table 3 show that nitrogen content descends significantly behind the stable hydrogenation, and the bromine valency is also reduced to very low, have reached the purpose of stable hydrogenation.The data of table 4～6 show that the smoke point of hydrogenation upgrading charging is very low, has only 11mm, has reached 23mm after the hydrogenation upgrading, and density is greater than 0.84g/cm
3, character such as flash-point, freezing point also meet the index request of big proportion aviation kerosene.With the liquefied coal coil raw material serves as to calculate benchmark, and the yield of aviation kerosene is up to 36 heavy %.
The stock oil character of table 1, stable hydrogenation step
| Analysis project | Analytical results |
| Density (20 ℃), g/cm 3 | 0.9362 |
| Basic n content, ppm | 1430 |
| S，ppm | 459 |
| N，ppm | 2027 |
| O，m％ | 1.58 |
| The bromine valency, gBr/100g | 17.49 |
| Boiling range (ASTM D-86), ℃ | |
| Initial boiling point/5% | 168/211 |
| 10％/20％ | 225/243 |
| 30％/50％ | 256/277 |
| 70％/80％ | 311/327 |
| 90%/do | 359/407 |
Table 2, stable hydrogenation reaction conditions
| Processing parameter | Guard reactor | The stable hydrogenation main reactor |
| The hydrogen dividing potential drop, Mpa | 10.0 | 10.0 |
| Temperature of reaction, ℃ | 330 | 350 |
| The host volume space velocity, h -1 | 12.5 | 2.5 |
| Hydrogen-oil ratio, v/v | 600 | 600 |
Table 3, stable hydrogenation product characteristics
| Analysis project | Analytical results |
| Density (20 ℃), g/cm 3 | 0.9104 |
| Basic n content, ppm | 589 |
| S，ppm | 22 |
| N，ppm | 635 |
| The bromine valency, gBr/100g | 2.9 |
| Boiling range (ASTM D-86), ℃ | |
| Initial boiling point/5% | 147/183 |
| 10％/20％ | 202/228 |
| 30％/50％ | 247/270 |
| 70％/80％ | 300/317 |
| 90%/do | 349/402 |
Table 4, hydrogenation upgrading feed properties
| Analysis project | Numerical value |
| Density (20 ℃), g/cm 3 | 0.8580 |
| Refractive power, nD 20 | 1.4560 |
| S，ppm | 295 |
| N，ppm | 553 |
| Smoke point, | 11 |
| Boiling range (ASTM D-86), ℃ | |
| Initial boiling point/5% | 152/167 |
| 10％/20％ | 173/183 |
| 30％/50％ | 186/204 |
| 70％/80％ | 213/220 |
| 90％/FBP | 241/278 |
The reaction conditions of table 5, hydrogenation upgrading
| Processing parameter | First reactor | Second reactor |
| Temperature of reaction, ℃ | 365 | 370 |
| Reaction pressure, MPa | 10.0 | 10.0 |
| Volume space velocity, h -1 | 0.5 | 0.5 |
| Hydrogen-oil ratio, v/v | 1000 | 1000 |
Aviation kerosene cut character after table 6, the hydrogenation upgrading
| Aviation kerosene cut character | Numerical value |
| Density (20 ℃), g/cm 3 | 0.8491 |
| Refractive power, nD 20 | 1.4488 |
| S，ppm | ＜5.0 |
| N，ppm | ＜5.0 |
| Smoke point, | 23 |
| Flash-point (remaining silent), ℃ | 58 |
| Freezing point, ℃ | ＜-47 |
| Aromatic hydrocarbons (FIA), volume % | 2.5 |
| Boiling range (ASTM D-86), ℃ | |
| IBP/5％ | 149/164 |
| 10％/20％ | 169/180 |
| 30％/50％ | 182/199 |
| 70％/80％ | 208/214 |
| 90％/FBP | 237/271 |
Claims (10)
1, a kind of method of producing big proportion aviation kerosene from the liquefied coal coil maximum is characterized in that this method comprises the following steps:
Liquefied coal coil is introduced into guard reactor; contact with hydrogen, protective material; the reaction effluent of guard reactor enters the stable hydrogenation main reactor; contact with hydrogen, stabilized hydrogenation catalyzer; the middle cut that the reaction effluent of stable hydrogenation main reactor obtains through separation enters hydrogenation upgrading reactor; contact with hydrogen, Hydrobon catalyst, hydrogenation upgrading catalyzer, the reaction effluent of hydrogenation upgrading reactor obtains aviation kerosene through separation.
2, according to the method for claim 1; it is characterized in that described protective material is VIB or VIII family non-precious metal catalyst or their combination that loads on unformed aluminum oxide or the silica-alumina supports; wherein the group vib metal is selected from Mo or/and W, and VIII family metal is selected from Co or/and Ni.
3,, it is characterized in that described guard reactor adopts the upflowing operation according to the method for claim 1.
4, according to the method for claim 1, the volume that it is characterized in that described guard reactor is 5～30% of a stable hydrogenation main reactor.
5,, it is characterized in that the reaction conditions of described guard reactor is: hydrogen dividing potential drop 3.0～30.0MPa according to the method for claim 1; 220～400 ℃ of temperature of reaction; Liquid hourly space velocity 0.2～20h
-1, hydrogen-oil ratio 200～2500v/v.
6, according to the method for claim 1, it is characterized in that the reaction conditions of described stable hydrogenation main reactor: hydrogen dividing potential drop 3.0～30.0MPa; 270～450 ℃ of temperature of reaction; Liquid hourly space velocity 0.1～10h
-1, hydrogen-oil ratio 300～2800v/v.
7, according to the method for claim 1, it is characterized in that described Hydrobon catalyst is a carrier with unformed aluminum oxide or sial, loaded metal component on it, metal component is VIB or VIII family non-precious metal catalyst or their combination, wherein the group vib metal is selected from Mo or/and W, and VIII family metal is selected from Co or/and Ni.
8, according to the method for claim 1, it is characterized in that the be combined as carrier of described hydrogenation upgrading catalyzer with unformed aluminum oxide or sial or they, loaded metal component on it, metal component is VIB or VIII family non-precious metal catalyst or their combination, wherein the group vib metal is selected from Mo or/and W, and VIII family metal is selected from Co or/and Ni.
9, according to the method for claim 1, it is characterized in that Hydrobon catalyst and hydrogenation upgrading catalyst loading are in a reactor, top filling Hydrobon catalyst, bottom filling hydrogenation upgrading catalyzer, the reaction conditions of this reactor is: hydrogen dividing potential drop 3.0～30.0MPa; 270～450 ℃ of temperature of reaction; Liquid hourly space velocity 0.1～10h
-1, hydrogen-oil ratio 500～3000v/v.
10, according to the method for claim 1, it is characterized in that Hydrobon catalyst and hydrogenation upgrading catalyzer are seated in respectively in two reactors, first reactor charge Hydrobon catalyst, second reactor charge hydrogenation upgrading catalyzer, the volume ratio of first reactor catalyst and second reactor catalyst is 1: 1～10: 1, and the reaction conditions of first reactor is: hydrogen dividing potential drop 3.0～30.0MPa; 270～450 ℃ of temperature of reaction; Liquid hourly space velocity 0.1～10h
-1, hydrogen-oil ratio 500～3000v/v; The reaction conditions of second reactor is: hydrogen dividing potential drop 3.0～30.0MPa; 280～450 ℃ of temperature of reaction; Liquid hourly space velocity 0.1～20h
-1, hydrogen-oil ratio 500～3000v/v.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100839008A CN100419044C (en) | 2005-07-15 | 2005-07-15 | Production of large-specific-weight aircraft liquid petroleum oil at maximum from coal liquefied oil |
| MYPI20063383 MY142269A (en) | 2005-07-15 | 2006-07-14 | A process for producing a high density jet fuel from a coal liquefied oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100839008A CN100419044C (en) | 2005-07-15 | 2005-07-15 | Production of large-specific-weight aircraft liquid petroleum oil at maximum from coal liquefied oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1896189A true CN1896189A (en) | 2007-01-17 |
| CN100419044C CN100419044C (en) | 2008-09-17 |
Family
ID=37608839
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005100839008A Active CN100419044C (en) | 2005-07-15 | 2005-07-15 | Production of large-specific-weight aircraft liquid petroleum oil at maximum from coal liquefied oil |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN100419044C (en) |
| MY (1) | MY142269A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102304387A (en) * | 2011-08-04 | 2012-01-04 | 神华集团有限责任公司 | Production method of coal-based high-density jet fuel |
| CN103194281A (en) * | 2013-04-18 | 2013-07-10 | 中国人民解放军空军油料研究所 | Coal-based mixed jet fuel |
| CN105441127A (en) * | 2014-09-30 | 2016-03-30 | 中国石油化工股份有限公司 | Method for producing jet fuel |
| CN108865263A (en) * | 2018-06-22 | 2018-11-23 | 煤炭科学技术研究院有限公司 | A kind of coal base mixing high energy density fuel and preparation method thereof |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0321713B1 (en) * | 1987-12-21 | 1993-03-10 | Abb Lummus Crest Inc. | Production of high density jet fuel from coal liquids |
| CN1162516C (en) * | 2002-02-07 | 2004-08-18 | 中国石油化工股份有限公司 | Process for greatly preparing hihg-quality diesel oil or jet fuel from liquefied coil oil |
| CN1224677C (en) * | 2002-10-30 | 2005-10-26 | 中国石油化工股份有限公司 | Composite process of producing high quality diesel oil from coal liquified oil |
-
2005
- 2005-07-15 CN CNB2005100839008A patent/CN100419044C/en active Active
-
2006
- 2006-07-14 MY MYPI20063383 patent/MY142269A/en unknown
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102304387A (en) * | 2011-08-04 | 2012-01-04 | 神华集团有限责任公司 | Production method of coal-based high-density jet fuel |
| CN102304387B (en) * | 2011-08-04 | 2014-07-02 | 神华集团有限责任公司 | Production method of coal-based high-density jet fuel |
| CN103194281A (en) * | 2013-04-18 | 2013-07-10 | 中国人民解放军空军油料研究所 | Coal-based mixed jet fuel |
| CN105441127A (en) * | 2014-09-30 | 2016-03-30 | 中国石油化工股份有限公司 | Method for producing jet fuel |
| CN105441127B (en) * | 2014-09-30 | 2017-06-30 | 中国石油化工股份有限公司 | A kind of method for producing jet fuel |
| CN108865263A (en) * | 2018-06-22 | 2018-11-23 | 煤炭科学技术研究院有限公司 | A kind of coal base mixing high energy density fuel and preparation method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| MY142269A (en) | 2010-11-15 |
| CN100419044C (en) | 2008-09-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100434496C (en) | Two-way combined process of wax-oil hydrogenation treatment and catalytic cracking | |
| CN103013559B (en) | Hydrocracking method for selective increasing of aviation kerosene yield | |
| CN1876767B (en) | Coal tar hydrocracking method | |
| CN100558863C (en) | A kind of combined method of producing cleaning oil from coal-tar oil | |
| CN101210198A (en) | Hydrogenation method for producing high grade diesel oil and high grade reforming raw material | |
| CN102399586A (en) | A mid-pressure hydrocracking method for producing jet fuel | |
| CN103305269B (en) | Method for producing gasoline and diesel by directly hydrogenating medium and low temperature coal tar | |
| CN102304387A (en) | Production method of coal-based high-density jet fuel | |
| CN104277879B (en) | A kind of two-stage slurry bed system hydrogenation technique of middle coalite tar | |
| CN1940030A (en) | Hydrogenation cracking method of high-output diesel oil from high-nitrogen content heavy raw material | |
| CN100419044C (en) | Production of large-specific-weight aircraft liquid petroleum oil at maximum from coal liquefied oil | |
| CN105713662A (en) | Hydrotreating and catalytic cracking combined process | |
| CN1896181A (en) | Production of high-bioctyl-value diesel oil by coal liquification | |
| CN102311782B (en) | Method for producing diesel oil by purifying coal tar through hydrogenating | |
| CN100351346C (en) | Medium pressure hydrocracking process for preparing jet fuel | |
| CN101376841A (en) | Heavy fraction oil hydrotreating method | |
| CN100510022C (en) | Low-hydrogenloss hydrogenation of high-output qulified diesel oil | |
| CN101376840A (en) | Heavy fraction oil hydrotreating method | |
| CN1211468C (en) | Hydrocracking method for increasing quality of refined diesel oil | |
| CN114456842B (en) | Production system and production method of high-quality distillate oil | |
| CN106520197B (en) | A kind of method for hydrogen cracking that boat coal is produced by inferior feedstock oil | |
| CN100594232C (en) | Inferior fraction oil upgrading process | |
| CN104419461B (en) | The slurry bed system of a kind of coal tar and fixed bed serial hydrogenation technique | |
| CN1261544C (en) | Medium pressure hydrogenation method for maximumly producing high quality diesel fuel | |
| CN109777499B (en) | Refinery gas combined processing technology |
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 |