CN1097210A - Produce the method for diesel oil with middle coalite tar - Google Patents
Produce the method for diesel oil with middle coalite tar Download PDFInfo
- Publication number
- CN1097210A CN1097210A CN 93107496 CN93107496A CN1097210A CN 1097210 A CN1097210 A CN 1097210A CN 93107496 CN93107496 CN 93107496 CN 93107496 A CN93107496 A CN 93107496A CN 1097210 A CN1097210 A CN 1097210A
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- China
- Prior art keywords
- oil
- diesel oil
- solution
- reaction
- coalite tar
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
- F02B3/00—Engines characterised by air compression and subsequent fuel addition
- F02B3/06—Engines characterised by air compression and subsequent fuel addition with compression ignition
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides the method that coalite tar is produced diesel oil in a kind of usefulness.It is removal of impurities that the present invention adopts the direct chemical purifying method, and---refining---washing---breakdown of emulsion---is allocated, and the water in middle coalite tar and the waste liquid is mixed separated with useless component, and refining goes out to reach the coal tar diesel oil of GB.The present invention does not need the customizations construction equipment, and technology is simple, with short production cycle, invest little instant effect, and by product also can fully utilize, for country saves a large amount of energy.
Description
The invention provides the method that coalite tar is produced diesel oil in a kind of the utilization.
China is the petroleum resources poorness on the one hand, and the production of diesel oil must utilize petroleum resources, has increased the consumption of petroleum-based energy.Another side has been wasted a large amount of energy again on existing coking industry, also cause the pollution to farmland, mining area and the Nature simultaneously.
The refinery practice of existing coal tar adopts distillation, hydrocracking, method productions such as liquid-phase catalysis cracking, because of facility investment higher, the processing condition complexity, the organic acid in the oil is indivisible, has limited the utilization of coal tar waste liquid.
The object of the present invention is to provide a kind of distillation of saving, the cracking program adopts the direct chemical method of refining, the water in middle coalite tar and the waste liquid is mixed separated with useless component, purifies and produces the method for diesel oil.
The present invention need not utilize the customizations construction equipment, and technology is simple, and is with short production cycle, invests little instant effect, and by product also can fully utilize, and coalite tar and tar waste liquid in fully effectively utilizing are for country saves a large amount of energy.
It is that removal of impurities-refining-washing-breakdown of emulsion-allotment is purified to the diesel oil that reaches GB with middle coalite tar and waste liquid that the present invention adopts the direct chemical method of refining, its technical process comprises and washes rough coal tar earlier with water and dewater, moisture content is reduced to below 10%, add the sulfuric acid (H of 95-98% then
2SO
4) carry out acid treatment and remove impurity, add the further removal of impurities alkali cleaning of sodium hydroxide (NaOH) of 10-30%, use the sodium bicarbonate (NaHCO of 5-20% again
3) solution (perhaps NaOH: NaHCO
3=1: 1-3: 1 mixed solution) carry out neutralization reaction, residual impurity is removed the back form essential oil, with the FeCl of 5-10%
3The solution washing essential oil, and utilize settlement separate method that impurity remaining in the oil is removed, carry out chemical demulsification with 1% ethanol (Nacl, the saltcake) aqueous solution, use CaCl
2Drying and dehydrating can extract the diesel oil that cetane value and flash-point reach GB with diesel-dope allotment at last.
Fig. 1 is a process flow sheet of the present invention.
1 couple of the present invention elaborates below in conjunction with accompanying drawing.
The present invention is 2: 1 amount ratio washing rough coal tar with oil and water ratio earlier and carries out processed, moisture content reduced to below 10%, with the sulfuric acid (H of 95-98% concentration
2SO
4) in oily: acid=2: 1-5: 1 ratio adds the acid treatment jar Central Shanxi Plain, make acid and oil after fully reacting 0.5-1 hour under the 10-60 ℃ of temperature, left standstill 4-24 hour, after getting rid of acid sludge, acid oil is introduced the alkaline purification jar, by oil: the amount ratio of water=3: 1 is introduced the alkaline purification jar with water, make water fully contact 15-20 minute with acid oil, left standstill 1-4 hour, get rid of water assorted after, with 10-30% sodium hydroxide (NaOH) solution by oil: alkali=20: 1-40: 1 ratio is introduced the alkaline purification jar, is to make alkali lye oilyly fully contact 0.5-1 hour with washing under the 10-70 ℃ of condition in temperature of reaction, leave standstill after 8-24 hour and be divided into two-phase, the upper strata is an alkali cleaning oil, and lower floor is the alkali cleaning slag, after eliminating lower floor alkali is assorted, alkali oil is introduced neutralization tank, and by oily: alkali lye=2: 1-5: 1 amount ratio adds the sodium bicarbonate (NaHCO of 5-10%
3) solution, be fully to react under the 10-70 ℃ of condition (perhaps to adopt NaOH: NaHCO in 0.5-1 hour in temperature
3=1: 1-3: 1 mixed solution, temperature of reaction are 10-50 ℃) after, reach fully neutralization, left standstill 1-8 hour, be divided into that to get rid of lower layer of water after the two-phase assorted, change upper strata neutral oil over to the dehydration cleaning of evaporator, with the FeCl of 5-10%
3Solution is pressed FeCl
3: oil=1: 20-1: 40 ratios are under the 90-98 ℃ of condition in temperature of reaction, react 0.5-1 hour, and the washing essential oil is got rid of remaining impurity in the oil.With 1% ethanol (Nacl, saltcake) aqueous solution is in washing lotion: oil=1: 10=1: 20 ratios are carried out chemical demulsification and washing, change dehydrated oil over to blend tank, left standstill 1-8 hour, it is assorted to get rid of water, adds the diesel-dope of 0.05-1% in the dehydrated oil behind the alkali breast, allocate, obtain the diesel oil processed oil that cetane value and flash-point etc. reach GB, it is standby to store storage tank into, and the leading indicator of processed oil can reach:
Cetane value 51, flash-point 61, density 0.8494
Boiling range: 242 ℃ of 50% recovered temperatures
329 ℃ of 90% recovered temperatures
368 ℃ of 95% recovered temperatures
Claims (7)
1, the method that coalite tar is produced diesel oil in a kind of usefulness, it is characterized in that: it is that coal tar diesel oil is produced in removal of impurities-refining-washing-breakdown of emulsion-allotment that this method adopts the direct chemical purifying method, comprise and wash rough coal tar with water and dewater, moisture content is reduced to below 10%, add the sulfuric acid (H of 95%-98% then
2SO
4) carry out acid treatment and remove impurity, add sodium hydroxide (NaOH) the solution removal of impurities alkali cleaning of 10-30%, with the sodium bicarbonate (NaHCO of 5-20%
3) solution (perhaps NaOH: NaHCO
3=1: 1-3: 1 mixed solution) carry out neutralization reaction, residual impurity is removed the back form essential oil, with the FeCl of 5-10%
3The solution washing essential oil, and utilize settlement separate method that impurity remaining in the oil is removed, use 1% ethanol (NaCl, the saltcake) aqueous solution to carry out chemical demulsification again, use CaCl
2Drying and dehydrating can extract the diesel oil that cetane value and flash-point etc. reach GB with the diesel-dope allotment at last.
2, produce the method for diesel oil by coalite tar in the described usefulness of claim 1, it is characterized in that: the crude oil of adding and sulfuric acid ratio are 2: 1-5: 1, and temperature of reaction is 10-60 ℃, the reaction times is 0.5-1 hour.
3, produce the method for diesel oil by coalite tar in the described usefulness of claim 1, it is characterized in that: the sodium hydroxide of adding (NaOH) solution and crude oil ratio are 1: 20-1: 40, and temperature of reaction is 10-70 ℃, the reaction times is 0.5-1 hour.
4, produce the method for diesel oil by coalite tar in the described usefulness of claim 1, it is characterized in that: the sodium bicarbonate (NaHCO of adding
3) solution and crude oil ratio be 1: 2-1: 5 temperature of reaction are 10-70 ℃, the reaction times be 0.5-1 hour (if adopt NaOH and NaHCO
3The mixed solution temperature of reaction is 10-50 ℃).
5, produce the method for diesel oil by coalite tar in the described usefulness of claim 1, it is characterized in that: add iron(ic) chloride (FeCl
3) solution with oil amount ratio be 1: 20-1: 40, temperature of reaction is 90-98 ℃, the reaction times is 0.5-1 hour.
6, produce the method for diesel oil by coalite tar in the described usefulness of claim 1, it is characterized in that: the ratio of the ethanol of adding (NaCl, saltcake) solution and crude oil is 1: 10-1: 20.
7, produce the method for diesel oil by coalite tar in the described usefulness of claim 1, it is characterized in that: diesel-dope and crude oil ratio are 0.05-1%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN93107496A CN1046310C (en) | 1993-07-03 | 1993-07-03 | Method for production of diesel fuel by using middle-low temp. coal tar |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN93107496A CN1046310C (en) | 1993-07-03 | 1993-07-03 | Method for production of diesel fuel by using middle-low temp. coal tar |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1097210A true CN1097210A (en) | 1995-01-11 |
| CN1046310C CN1046310C (en) | 1999-11-10 |
Family
ID=4986716
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN93107496A Expired - Fee Related CN1046310C (en) | 1993-07-03 | 1993-07-03 | Method for production of diesel fuel by using middle-low temp. coal tar |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1046310C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1109089C (en) * | 2000-12-22 | 2003-05-21 | 昆明市西山区长胜能源开发燃料油厂 | Process for preparing heavy coal tar from high-temp coal tar |
| CN102304378A (en) * | 2011-08-19 | 2012-01-04 | 孙成忠 | Low and medium temperature coal tar cold cutting separation method |
| CN102399583A (en) * | 2011-10-17 | 2012-04-04 | 河南省汤阴县永新助剂厂 | Recycling process of solvent naphtha in anti-scorching agent CTP production |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103937531A (en) * | 2014-03-27 | 2014-07-23 | 中国石油天然气集团公司 | Chemical pretreatment agent and pretreatment method for coal tar |
-
1993
- 1993-07-03 CN CN93107496A patent/CN1046310C/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1109089C (en) * | 2000-12-22 | 2003-05-21 | 昆明市西山区长胜能源开发燃料油厂 | Process for preparing heavy coal tar from high-temp coal tar |
| CN102304378A (en) * | 2011-08-19 | 2012-01-04 | 孙成忠 | Low and medium temperature coal tar cold cutting separation method |
| CN102304378B (en) * | 2011-08-19 | 2013-03-27 | 孙成忠 | Low and medium temperature coal tar cold cutting separation method |
| CN102399583A (en) * | 2011-10-17 | 2012-04-04 | 河南省汤阴县永新助剂厂 | Recycling process of solvent naphtha in anti-scorching agent CTP production |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1046310C (en) | 1999-11-10 |
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| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: HU PING Free format text: FORMER NAME OR ADDRESS: HU WENXUE |
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| CP03 | Change of name, title or address |
Address after: 650202 Yunnan Province, Kunming city Guandu District, Kunming beer factory Patentee after: Hu Ping Address before: 650201 Yunnan electron tube factory Patentee before: Hu Wenxue |
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| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |