CN1074039C - Producing technology for refined jet fuel - Google Patents
Producing technology for refined jet fuel Download PDFInfo
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- CN1074039C CN1074039C CN97101474A CN97101474A CN1074039C CN 1074039 C CN1074039 C CN 1074039C CN 97101474 A CN97101474 A CN 97101474A CN 97101474 A CN97101474 A CN 97101474A CN 1074039 C CN1074039 C CN 1074039C
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Abstract
The present invention discloses a production process for refined jet fuel, which relates to a method for decolouring and refining jet fuel. The production process adopts the common hydrofining to prepare a used catalyst. Raw materials are sent into a reaction tower by a pump, and react in the reaction tower. Then, reaction products are separated in a separate tower. After the reaction products are stripped by gas in a gas stripping tower, a finished product is prepared. The production process is characterized in that the reaction temperature in the reaction tower is from 40 to 180 DEG C. The production process has the advantages that jet fuel after being refined at low temperature has good color, moderate process conditions, small energy consumption and little reaction heat; when the production process is applied to industry, a reaction bed basically has no temperature rise.
Description
The present invention relates to the method for decolorizing and refining of rocket engine fuel.
At present, China Guangzhou general petrochemicals factory of producer of hydrogenation method refined jet fuel, its hydrofining technology condition is: hydrogen dividing potential drop: 0.7-2.5MPa; Temperature (℃): 200-310; Hydrogen-oil ratio (V/V), 50-200:1; Volume space velocity (h
-1): 1-8; Use common Hydrobon catalyst.When adopting the hydrogenation method refined jet fuel, general theory thinks that temperature is more than 200 ℃, and the hydrofining effect is relatively poor in the time of below 200 ℃.Its weak point is: temperature of reaction is had relatively high expectations, and has increased production cost.
Purpose of the present invention just provides a kind of production technique of refined jet fuel, and its technical process is simple, and temperature of reaction is lower, and it is good to face the rocket engine fuel color of hydrogen after refining, and energy consumption is little, reaction heat seldom, the reaction bed temperature rise after the industrialization is seldom.
A kind of producing technology for refined jet fuel, it adopts the smart employed catalyzer of general hydrogenation, raw material is squeezed into reaction tower through pump, in reaction tower, react, in knockout tower, separate then, be finished product after gas is carried in gas stripping column, it is characterized in that: raw material is selected the 2# rocket engine fuel for use, the base oil of 3# rocket engine fuel or 3# rocket engine fuel; Reaction conditions in reaction is taken is: temperature of reaction 40-180 ℃, the reactive hydrogen dividing potential drop is 0.7-2.5MPa, and hydrogen-oil ratio is 50-200:1 by volume, and volume space velocity is 1-8h
-1Separation condition is in knockout tower: hydrogen pressure is 0.7-2.5MPa, and temperature is 40-180 ℃; Gas in gas stripping column is put forward condition: pressure 0.7-2.5MPa, temperature is 40-180 ℃.Said catalyzer is; Wi-W type or Wi-NO type Hydrobon catalyst.
The invention has the advantages that: the rocket engine fuel color behind the low-temperature purifying method is good, and processing condition relax, and energy consumption is little, and reaction heat seldom; During industrial application, reaction bed does not have temperature rise substantially.
Principle of work: with the RN-1 catalyzer is example, temperature when lesser temps≤80 ℃, and the R8-1 catalyzer mainly is to show as adsorption bleaching, and along with the increase of catalyzer absorption saturation ratio, its decolouring is active to descend, and it is shorter therefore to show as life of catalyst.Temperature is more than or equal to 120 ℃ when at comparatively high temps, and during smaller or equal to 180 ℃, this catalyzer trace impurity in the raw material such as colloid under facing the hydrogen state are removed by hydrogenation, a spot of unsaturated hydrocarbons by saturated as alkene etc., thereby improve the color of raw material, the decolouring activity that shows as catalyzer in its test-results is very stable, and the stability test of catalyzer is more than 2000 hours, during industrial application, life of catalyst is 1-3.Test-results sees attached list one.
Subordinate list one is character synopsis before and after the feed purification of the present invention
Base oil a part sieve essential oil with the 3# rocket engine fuel is a raw material, raw material is squeezed into reaction tower through pump, in reaction tower, react, in knockout tower, separate then, be finished product after gas is carried in gas stripping column, the reaction conditions in reaction tower is: temperature is 150 ℃, and the hydrogen dividing potential drop is 1.0MPa, volume space velocity is 5h-1, and hydrogen to oil volume ratio is 50: 1; Separation condition is in knockout tower, hydrogen pressure 0.7-2.5MPa, and temperature is 40-180 ℃; It is pressure 0.7-2.5MPa that gas in gas stripping column is put forward condition, and temperature is 40-180 ℃.Subordinate list one:
| Project | Molecular sieve essential oil raw material | Refining back product | |
| Total sulfur (PPa) content | 35.2 | 34.8 | |
| Total nitrogen (PPa) content | ＜1 | ＜1 | |
| Iodine number (g iodine/100g) | 0.6 | 0.24 | |
| Colloid (a/a) content | 0.31％ | 0.24％ | |
| Aromatic hydrocarbons (a/a) content | Monocycle | 14.93％ | 14.70％ |
| Dicyclo | 0.64％ | 0.61％ | |
| Many rings | 540PPa | 524PPa | |
| Total aromatic hydrocarbons (a/a) content | 15.524％ | 15.362％ | |
| Color (number) | +21 | +28 | |
Claims (1)
1, a kind of producing technology for refined jet fuel, it adopts the smart employed catalyzer of general hydrogenation, raw material is squeezed into reaction tower through pump, in reaction tower, react, in knockout tower, separate then, be finished product after gas is carried in gas stripping column, it is characterized in that: raw material is selected the 2# rocket engine fuel for use, the base oil of 3# rocket engine fuel or 3# rocket engine fuel; Reaction conditions in reaction is taken is: temperature of reaction 40-180 ℃, the reactive hydrogen dividing potential drop is 0.7-2.5MPa, and hydrogen-oil ratio is 50-200 by volume: 1, and volume space velocity is 1-8h
-1Separation condition is in knockout tower: hydrogen pressure is 0.7-2.5MPa, and temperature is 40-180 ℃; It is pressure 0.7-2.5MPa that gas in gas stripping column is put forward condition, and temperature is 40-180 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97101474A CN1074039C (en) | 1997-03-24 | 1997-03-24 | Producing technology for refined jet fuel |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97101474A CN1074039C (en) | 1997-03-24 | 1997-03-24 | Producing technology for refined jet fuel |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1194295A CN1194295A (en) | 1998-09-30 |
| CN1074039C true CN1074039C (en) | 2001-10-31 |
Family
ID=5165763
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97101474A Expired - Fee Related CN1074039C (en) | 1997-03-24 | 1997-03-24 | Producing technology for refined jet fuel |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1074039C (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1061617A (en) * | 1990-11-20 | 1992-06-03 | 杨家振 | A kind of prescription of coal-tar type diesel and compound method |
| CN1110986A (en) * | 1994-04-28 | 1995-11-01 | 湖南长泰能源实业有限公司 | Prodn. technique and Equipment for epuration and prepn. of domestic fuel by utilizing carbon 5 cut |
| CN1138083A (en) * | 1995-06-14 | 1996-12-18 | 中国石油化工总公司石油化工科学研究院 | Method for production of light fuel and lubricating oil with high viscosity index |
-
1997
- 1997-03-24 CN CN97101474A patent/CN1074039C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1061617A (en) * | 1990-11-20 | 1992-06-03 | 杨家振 | A kind of prescription of coal-tar type diesel and compound method |
| CN1110986A (en) * | 1994-04-28 | 1995-11-01 | 湖南长泰能源实业有限公司 | Prodn. technique and Equipment for epuration and prepn. of domestic fuel by utilizing carbon 5 cut |
| CN1138083A (en) * | 1995-06-14 | 1996-12-18 | 中国石油化工总公司石油化工科学研究院 | Method for production of light fuel and lubricating oil with high viscosity index |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1194295A (en) | 1998-09-30 |
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