CN102250654A - Method for manufacturing oil from coal - Google Patents
Method for manufacturing oil from coal Download PDFInfo
- Publication number
- CN102250654A CN102250654A CN2011101542117A CN201110154211A CN102250654A CN 102250654 A CN102250654 A CN 102250654A CN 2011101542117 A CN2011101542117 A CN 2011101542117A CN 201110154211 A CN201110154211 A CN 201110154211A CN 102250654 A CN102250654 A CN 102250654A
- Authority
- CN
- China
- Prior art keywords
- coal
- oil
- solvent
- coal dust
- high temperature
- 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.)
- Pending
Links
Abstract
The invention relates to a method for manufacturing oil from coal, and the method is mainly characterized by comprising the following steps: (a) a coal powder preparing step; (b) a coal slurry preparing step: 1) mixing the coal powder with a solvent and a catalyst in a weight ratio, and 2) sufficiently stirring with a stirrer to obtain the coal slurry; (c) a reaction kettle treatment step: conveying the coal slurry into a reaction kettle to react at a high temperature and high pressure for a certain reaction time to obtain liquefied oil, and using the liquefied oil as the solvent of step (b) during reproduction; (d) a distillation kettle treatment step: conveying the liquefied oil into a distillation kettle, and carrying out fractionation at a high temperature to obtain gasoline, crude diesel oil and oil residues; and (e) a filtering and blending agent adding step: filtering the crude diesel oil at normal temperature and normal pressure to remove impurities and then adding the blending agent in a weight ratio to obtain an oil finished product. The method provided by the invention has the advantages of easily available raw materials, simple process, no use of hydrogenation and hydrogen preparation equipment, low equipment investment and no environmental pollution; and the obtained product has low price and good market prospects, and is suitable for popularization.
Description
Technical field
The present invention relates to a kind of fuel preparation method, refer in particular to a kind of preparation method of a kind of power fuel of alternative prior art, say that more specifically the present invention is a kind of method of coal system oil.The present invention should be divided into C portion in International Patent Classification (IPC).
Background technology
Along with the development of world economy and the raising of human progress and life, increase gradually for the demand of power fuel, especially because traditional oil, natural gas source are day by day deficient, so seek the key that substitute energy will become the future world Economic development.Yet because relevant prior art is because of complex structure, invest too greatly, cost is too high, produces little effect at present, thereby causes the supply of fuel anxiety, and price improves, even lead to war, causes disaster to some geographic people.In addition, because the deficiency of existing fuel institute inherent defective and technology of preparing, the environment that also makes the earth obviously influences the eubiosis of the earth worse and worse, and species are quickening extinction, and human habitat degenerates.
Summary of the invention
The objective of the invention is to: at the deficiencies in the prior art, provide a kind of raw material easily to get, technology is simple, does not adopt hydrogenation and hydrogen producer, less investment, the method for a kind of coal system oil free from environmental pollution.
The objective of the invention is to be achieved through the following technical solutions:
The method of described coal system oil may further comprise the steps:
(1) system coal dust step
1) coal is broken into coal dust,
2) step 1) gained coal dust is sieved obtain satisfactory coal dust after removing impurity.
(2) system coal slurry step
1) above-mentioned satisfactory coal dust is mixed according to part by weight with solvent and catalyzer,
2) fully stir with stirrer and make coal slurry.
(3) reactor treatment step
1) above-mentioned gained coal slurry is sent in the reactor,
2) obtain liquefaction oil through reaction in 1.5-2 hour under high temperature, high pressure, this liquefaction oil can be used as the solvent in the step (two) when regeneration was produced.
(4) still kettle treatment step
The gained liquefaction oil is sent in the still kettle, increased temperature and fractionate out gasoline, gas oil and the dregs of fat.
(5) filtration and adding blender step
With resulting gas oil at normal temperatures and pressures, remove after filtration and add blender again according to weight proportion behind the impurity and promptly obtain processed oil.
Because the present invention has adopted above-mentioned technical scheme, the main raw material that is adopted is a coal, and cost greatly reduces; And resulting liquefaction oil can be used as solvent in the step (two) in the reactor treatment step, has created good condition for cyclic production further reduces cost; Owing to adopt not hydrogenation and hydrogen producer, facility investment is also quite few.In addition, the catalyst function in this method is fairly good; In addition, present method is free from environmental pollution, the product conformance with standard.
Embodiment
The present invention is further described below in conjunction with embodiment: the present invention includes (one) system coal dust step, (two) system coal slurry step, (three) reactor treatment step, (four) still kettle treatment step and (five) filtration and add blender step totally five treatment steps.Mainly be coal to be broken into coal dust sieve and obtain satisfactory coal dust after removing impurity in (one) step; In system coal dust step, in a specific embodiment, described satisfactory coal dust will be more than 200 orders.Mainly be that above-mentioned satisfactory coal dust is mixed according to part by weight with solvent and catalyzer in (two) step, fully stir with stirrer and make coal slurry; In described system coal slurry step: described catalyzer comprises zinc chloride, naphthane, hydrolith and ferric oxide; The part by weight of described coal dust and solvent and catalyzer is: coal dust 1000kg, solvent 300kg, zinc chloride 30kg, naphthane 30kg, hydrolith 30kg, ferric oxide 13kg.In (three) step, mainly be that above-mentioned gained coal slurry is sent in the reactor, obtain liquefaction oil through the little the reaction time of 1.5-2 under high temperature, high pressure, this liquefaction oil can be used as the solvent in the step (two) when regeneration was produced, and this can further reduce production costs; In specific embodiment, described high temperature is 410 ℃-450 ℃, and described high pressure is 11Mpa-20Mpa; Wherein said high temperature is 415 ℃-435 ℃, and described high pressure is that 12Mpa-17Mpa is better.In (four) step, mainly be that the gained liquefaction oil is sent in the still kettle, increase temperature and fractionate out gasoline, gas oil and the dregs of fat; Wherein the gained dregs of fat are the good materials that are used for brickmaking; In the still kettle treatment step, employed high temperature is 340 ℃-380 ℃.In (five) step, mainly be at normal temperatures and pressures with resulting gas oil, remove after filtration and add blender again according to weight proportion behind the impurity and promptly obtain processed oil; Described blender comprises: ferrocene, the positive butyl ester of nitric acid and isoamyl nitrate; In this step, the weight proportion of described gas oil and blender is: gas oil 1000kg, ferrocene 20g, the positive butyl ester 7kg of nitric acid, isoamyl nitrate 8kg.When beginning, used solvent is a heavy oil; When cyclic production, can use resulting liquefaction oil in step (three), thereby cost reduces greatly.The final resulting main products of the present invention is " 0 " number smart diesel oil.
Raw material of the present invention is easily got, and technology is simple, adopts not hydrogenation and hydrogen producer, and the production less investment is free from environmental pollution, and the product conformance with standard of making is cheap, and market outlook are good, are fit to promote the use of.
Claims (9)
1. the method for a coal system oil, it is characterized in that: the method for described coal system oil may further comprise the steps:
(1) system coal dust step
1) coal is broken into coal dust,
2) step 1) gained coal dust is sieved obtain satisfactory coal dust after removing impurity;
(2) system coal slurry step
1) above-mentioned satisfactory coal dust is mixed according to part by weight with solvent and catalyzer,
2) fully stir with stirrer and make coal slurry;
(3) reactor treatment step
1) above-mentioned gained coal slurry is sent in the reactor,
2) obtain liquefaction oil through reaction in 1.5-2 hour under high temperature, high pressure, this liquefaction oil can be used as the solvent in the step (two) when regeneration was produced;
(4) still kettle treatment step
The gained liquefaction oil is sent in the still kettle, increased temperature and fractionate out gasoline, gas oil and the dregs of fat;
(5) filtration and adding blender step
With resulting gas oil at normal temperatures and pressures, remove after filtration and add blender again according to weight proportion behind the impurity and promptly obtain processed oil.
2. the method for coal system oil according to claim 1 is characterized in that:
In described system coal dust step, described satisfactory coal dust is more than 200 orders.
3. the method for coal system oil according to claim 1 is characterized in that:
In described system coal slurry step:
Described catalyzer comprises zinc chloride, naphthane, hydrolith and ferric oxide,
The part by weight of described coal dust and solvent and catalyzer is: coal dust 1000kg, solvent 300kg, zinc chloride 30kg, naphthane 30kg, hydrolith 30kg, ferric oxide 13kg.
4. the method for coal system oil according to claim 1 is characterized in that:
In described reactor treatment step:
Described high temperature is 410 ℃-450 ℃, and described high pressure is 11Mpa-20Mpa.
5. according to the method for claim 1 or 4 described coal system oil, it is characterized in that:
Described high temperature is 415 ℃-435 ℃, and described high pressure is 12Mpa-17Mpa.
6. the method for coal system oil according to claim 1 is characterized in that:
In described still kettle treatment step:
Described high temperature is 340 ℃-380 ℃.
7. the method for coal system oil according to claim 1 is characterized in that:
In described filtration and adding blender step:
Described blender comprises: ferrocene, the positive butyl ester of nitric acid and isoamyl nitrate,
The weight proportion of described gas oil and blender is: gas oil 1000kg, ferrocene 20g, the positive butyl ester 7kg of nitric acid, isoamyl nitrate 8kg.
8. the method for coal system oil according to claim 1 is characterized in that:
Described solvent is a heavy oil.
9. the method for coal system oil according to claim 1 is characterized in that:
Described processed oil is " 0 " number smart diesel oil.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101542117A CN102250654A (en) | 2011-06-10 | 2011-06-10 | Method for manufacturing oil from coal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101542117A CN102250654A (en) | 2011-06-10 | 2011-06-10 | Method for manufacturing oil from coal |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102250654A true CN102250654A (en) | 2011-11-23 |
Family
ID=44978227
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011101542117A Pending CN102250654A (en) | 2011-06-10 | 2011-06-10 | Method for manufacturing oil from coal |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102250654A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105602601A (en) * | 2015-12-30 | 2016-05-25 | 金先奎 | Coal-to-oil catalytic extraction technology and special device thereof |
| CN106635109A (en) * | 2016-11-02 | 2017-05-10 | 新疆大学 | Method for increasing co-liquefaction conversion rate of low-rank coal/naphthenic base vacuum residue and diesel fraction content |
| CN106867550A (en) * | 2017-01-19 | 2017-06-20 | 沈阳新思维数控机床有限公司 | The method for preparing low-temperature catalyzed light fuel processed |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1515650A (en) * | 2004-01-08 | 2004-07-28 | 珠海市三金高科技产业有限公司 | Technological process for extracting liquid fuel from coal by utilizing hot-melt catalytic process |
| CN1587351A (en) * | 2004-07-30 | 2005-03-02 | 神华集团有限责任公司 | Method for directly liquefying coal |
| CN100999678A (en) * | 2007-01-04 | 2007-07-18 | 煤炭科学研究总院 | Directly hydrogenating liquifying process for mixed coal |
| CN101020834A (en) * | 2007-03-10 | 2007-08-22 | 江苏天一超细金属粉末有限公司 | Coal liquifying process based on pentacarbonyl iron as catalyst |
| CN101182421A (en) * | 2007-12-13 | 2008-05-21 | 肇庆市顺鑫煤化工科技有限公司 | Thermally dissolving and catalytic method for preparing liquid fuel by lignite as well as catalyst and solvent used therefor |
| CN101429440A (en) * | 2007-07-25 | 2009-05-13 | 汉能科技有限公司 | Method for direct liquefaction of coal |
| CN101565631A (en) * | 2009-06-02 | 2009-10-28 | 华东理工大学 | Method for directly liquefying coal in CO and H2O system |
-
2011
- 2011-06-10 CN CN2011101542117A patent/CN102250654A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1515650A (en) * | 2004-01-08 | 2004-07-28 | 珠海市三金高科技产业有限公司 | Technological process for extracting liquid fuel from coal by utilizing hot-melt catalytic process |
| CN1587351A (en) * | 2004-07-30 | 2005-03-02 | 神华集团有限责任公司 | Method for directly liquefying coal |
| CN100999678A (en) * | 2007-01-04 | 2007-07-18 | 煤炭科学研究总院 | Directly hydrogenating liquifying process for mixed coal |
| CN101020834A (en) * | 2007-03-10 | 2007-08-22 | 江苏天一超细金属粉末有限公司 | Coal liquifying process based on pentacarbonyl iron as catalyst |
| CN101429440A (en) * | 2007-07-25 | 2009-05-13 | 汉能科技有限公司 | Method for direct liquefaction of coal |
| CN101182421A (en) * | 2007-12-13 | 2008-05-21 | 肇庆市顺鑫煤化工科技有限公司 | Thermally dissolving and catalytic method for preparing liquid fuel by lignite as well as catalyst and solvent used therefor |
| CN101565631A (en) * | 2009-06-02 | 2009-10-28 | 华东理工大学 | Method for directly liquefying coal in CO and H2O system |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105602601A (en) * | 2015-12-30 | 2016-05-25 | 金先奎 | Coal-to-oil catalytic extraction technology and special device thereof |
| CN106635109A (en) * | 2016-11-02 | 2017-05-10 | 新疆大学 | Method for increasing co-liquefaction conversion rate of low-rank coal/naphthenic base vacuum residue and diesel fraction content |
| CN106867550A (en) * | 2017-01-19 | 2017-06-20 | 沈阳新思维数控机床有限公司 | The method for preparing low-temperature catalyzed light fuel processed |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102527405B (en) | Catalyst used in complete methanation of synthesis gas at high temperature and preparation method thereof | |
| CN103194606B (en) | Method for concentrating platinum group metals from alumina-based waste catalyst | |
| CN102600860B (en) | Catalyst suitable for complete methanation of middle-low-temperature synthetic gas and preparation method thereof | |
| CN102942972B (en) | Method for producing liquefied natural gas by coke oven gas | |
| CN101705105B (en) | Biomass liquified oil and preparation method thereof | |
| CN101444740A (en) | Catalyst for hydrogen production by bio-oil steam reforming and preparation method thereof | |
| CN102925178B (en) | Method for preparing iron alloy, calcium carbide and formed coke for gasification industry from low-metamorphic powdered coal | |
| CN102250654A (en) | Method for manufacturing oil from coal | |
| CN102218324A (en) | Catalyst for removing oxygen and improving quality of bio-oil and preparation method thereof | |
| CN108404918A (en) | Tumer ester through hydrogenation produces the copper zinc SiO 2 catalyst and preparation method thereof of ethyl alcohol | |
| CN114272932B (en) | Nickel-cerium biochar catalyst and preparation method and application thereof | |
| CN108300531B (en) | Composite briquette adhesive and preparation method thereof | |
| CN103980964A (en) | Preparation method of tourmalinite fuel oil activator | |
| CN110041951A (en) | A kind of needle coke and preparation method thereof | |
| CN110330993A (en) | A kind of briquetted coal blending coking method based on difunctional binder | |
| CN103834426A (en) | Method for producing liquefied oil by directly hydro-liquefy coal in presence of ionic liquid | |
| CN102994137B (en) | Method for preparing algae material fuel by catalytic liquefying method | |
| CN114621097B (en) | Method for preparing 2, 4-difluoroaniline by catalytic hydrogenation of 2, 4-difluoronitrobenzene | |
| CN110723747B (en) | Method for recovering and preparing high-quality zinc oxide from zinc waste | |
| CN101845315A (en) | Method for directly liquefying hydrogen-donating coal in situ at low pressure | |
| CN101440299A (en) | Method for preparing -10 DEC C biodiesel from waste lipid by distillation process | |
| CN101575530A (en) | Biomass liquefied oil and preparation method thereof | |
| CN111020182A (en) | Composite metallurgical pellet binder, cold-pressed pellet containing same and preparation method thereof | |
| CN109294612A (en) | A method of add hydrogen to prepare fuel oil altogether using sawdust and mink cell focus | |
| CN101935562B (en) | Synthetic diesel oil and preparation method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20111123 |