CN101597507B - Method for directly producing liquid hydrocarbon in coal oil-gas reservoir - Google Patents
Method for directly producing liquid hydrocarbon in coal oil-gas reservoir Download PDFInfo
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- CN101597507B CN101597507B CN2008101143030A CN200810114303A CN101597507B CN 101597507 B CN101597507 B CN 101597507B CN 2008101143030 A CN2008101143030 A CN 2008101143030A CN 200810114303 A CN200810114303 A CN 200810114303A CN 101597507 B CN101597507 B CN 101597507B
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- 239000003245 coal Substances 0.000 title claims abstract description 93
- 238000000034 method Methods 0.000 title claims abstract description 49
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 35
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 35
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 32
- 239000007788 liquid Substances 0.000 title claims abstract description 32
- 239000000571 coke Substances 0.000 claims abstract description 30
- 238000006243 chemical reaction Methods 0.000 claims abstract description 19
- 238000004939 coking Methods 0.000 claims abstract description 14
- 239000003921 oil Substances 0.000 claims description 88
- 239000000446 fuel Substances 0.000 claims description 30
- 239000010742 number 1 fuel oil Substances 0.000 claims description 23
- 239000000203 mixture Substances 0.000 claims description 22
- 239000003318 humic coal Substances 0.000 claims description 12
- 239000002802 bituminous coal Substances 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 11
- 230000001698 pyrogenic effect Effects 0.000 claims description 11
- 239000003077 lignite Substances 0.000 claims description 9
- 239000011280 coal tar Substances 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims description 7
- 238000005984 hydrogenation reaction Methods 0.000 claims description 6
- 239000002904 solvent Substances 0.000 claims description 5
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 239000002817 coal dust Substances 0.000 claims description 4
- 238000000605 extraction Methods 0.000 claims description 4
- 238000004231 fluid catalytic cracking Methods 0.000 claims description 4
- 239000003079 shale oil Substances 0.000 claims description 4
- 238000004230 steam cracking Methods 0.000 claims description 4
- 239000011269 tar Substances 0.000 claims description 4
- 230000003111 delayed effect Effects 0.000 claims description 3
- 239000006185 dispersion Substances 0.000 claims description 2
- 239000012530 fluid Substances 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 28
- 239000001257 hydrogen Substances 0.000 abstract description 5
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract 1
- 239000003054 catalyst Substances 0.000 abstract 1
- 239000003250 coal slurry Substances 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 11
- 239000000463 material Substances 0.000 description 7
- 238000000197 pyrolysis Methods 0.000 description 5
- 238000004062 sedimentation Methods 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 239000003034 coal gas Substances 0.000 description 3
- 239000010779 crude oil Substances 0.000 description 3
- 239000001993 wax Substances 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000003502 gasoline Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 229910001021 Ferroalloy Inorganic materials 0.000 description 1
- 108010010803 Gelatin Proteins 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000010430 carbonatite Substances 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000003974 emollient agent Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 229920000159 gelatin Polymers 0.000 description 1
- 239000008273 gelatin Substances 0.000 description 1
- 235000019322 gelatine Nutrition 0.000 description 1
- 235000011852 gelatine desserts Nutrition 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229920000620 organic polymer Polymers 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000010117 shenhua Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
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Abstract
The invention relates to a method for directly producing liquid hydrocarbon in a coal oil-gas reservoir. Oil-coal-slurry is obtained by mixing coal and oil and enters a coking device for coking reaction under 480-510 DEG C so as to obtain coke, the liquid hydrocarbon and gases. Compared with the direct liquidation and the indirect liquidation of coal, the method has lower equipment investment and operation cost without consuming hydrogen and using catalyst and can obtain the liquid hydrocarbon with higher yield.
Description
Technical field
The invention belongs to a kind ofly under the situation that does not have hydrogen, the thermal non-catalytic cracking method of coal more particularly, is the method for a kind of coal through the coking production liquid hydrocarbon.
Background technology
At the beginning of last century, some external scholars just find olefiant phenomenon of coal and evidence, and people have begun the olefiant broad research of coal thereupon, and this research is development, the i.e. direct liquefaction of coal and indirect liquefaction in two directions.
The direct liquefaction of coal starts from Germany the earliest, and the history of last 100 years has been arranged so far.Just built up the DCL/Direct coal liquefaction factory of first industrial-scale production in the world the twenties in eighties of last century, had the production equipment of 11 cover direct liquefactions to put into production during the World War II again, working pressure at that time is up to 70MPa.Be the period of oil and natural gas great development the sixties in 20th century, and expensive DCL/Direct coal liquefaction seizes up basically, up to the seventies in last century; Because oil crisis, developed country begins the research of gelatin liquefaction again, to the character of different material coal, the kind of catalyzer and the formation of product; Four kinds of typical liquefaction process have been formed gradually; Promptly German IGOR technology, NEDOL technology, the HTI technology of the U.S. and the Shenhua technology of China of Japan.The direct liquefaction of coal needs hydrogenation, makes the organic polymer in the coal be converted into more low molecular liquid fuel, and reaction needed high pressure and high temperature.Even present so-called demulcent technology, its pressure is also up to 19～30MPa, and temperature is at 400～500 ℃.No matter the sort of technology, its reaction conditions all are very harsh.
The indirect liquefaction technology of coal also originates from Germany, by the imperial coal research of Germany Fischer and Tropsch invent, so it is synthetic to be called as F-T (fischer-tropsch).This process makes synthetic gas (CO+H with gasification earlier
2), synthetic gas is adjusted its H through purifying
2/ CO ratio synthesizes liquid fuel through F-T again.The advantage of ICL for Indirect Coal Liquefaction is the flexibility broad of coal, and operational condition relaxes relatively.9 cover production equipments are had altogether in Germany during the World War II.But the indirect liquefaction flow process of coal is long especially; Device and equipment are many especially; Build such factory and almost equal the summation of a producer gas plant and a refinery; Therefore the fixed investment expense is very high, and its total efficiency is high not as direct liquefaction, has only South Africa to have the factory of the ICL for Indirect Coal Liquefaction of scale the biggest in the world at present.
Also have a kind of coal oil refining process in addition, i.e. the low-temperature pyrolysis technology of coal, this technology originates in early in the twentieth century, mainly is for obtaining coal gas and from coal gas, reclaiming lower boiling hydro carbons material.This technology majority is a raw material with high volatile coals such as brown coal, sub-bituminous coals, and pyrolysis temperature is being called middle low-temperature pyrolysis below 600～700 ℃.The productive rate of coal gas is not high in the destructive distillation product, is generally 120～200m
3/ t dry coal, wherein H
2, CH
4Content is higher, reaches more than the 70 volume % calorific value 25～26MJ/m
3, be the fine domestic gas, also can be used as synthetic raw gas.The productive rate of liquid resultant generally is merely 6～12 weight %; Specific density is little, boiling point is low, and its composition is similar with the petroleum-type liquid hydrocarbon, but it is more to contain phenols; Also can obtain qualified gasoline, diesel oil, paraffin and asphaltic products. through hydrogenation, reformation; Solids after the destructive distillation is called semicoke, and its intensity is low, piece is little, can be as the raw material of ferroalloy smelting with Jiao, smokeless fuel or formed coke.The productive rate of this method liquid hydrocarbon is very low.
Summary of the invention
Be that main hydrocarbons is not only composed and is stored in sandstone or the carbonatite space medium with the low molecular compound; Constitute the hydrocarbon-bearing pool of traditional concept, also be stored in and give birth to hydrocarbon, but be difficult for maybe can not arranging hydrocarbon; And can be used as among the special coal petrography that preserves medium, constitute " coal oil-gas reservoir ".In coal oil-gas reservoir, hydrocarbons mainly is to be melted in mutually among the miniature reservoir space between the coal petrography macromolecular mass with fused, or is adsorbed on the surface in coal petrography crack or space.
The objective of the invention is on the basis of above-mentioned discovery, to provide a kind of method from coal oil-gas reservoir direct production liquid hydrocarbon.
Technical scheme of the present invention is following:
A kind of method from coal oil-gas reservoir direct production liquid hydrocarbon obtains coal oil mixture with coal and oils mixing, and coal oil mixture gets into coker, under 480～510 ℃, carries out pyrogenic reaction, obtains coke, liquid hydrocarbon and gas.
Said coal is a humic coal or/and sapropelinite, and wherein humic coal is brown coal or/and bituminous coal, bituminous coal be selected from long-flame coal, in the sticking coal, weakly caking coal one or more, sapropelinite is selected from one or more in algal coal, moss coal, the cannel coal.Preferred coal is brown coal, in the bituminous coal in the humic coal one or more in sapropelinite, the humic coal.
The volatile matter of said coal is greater than 30 heavy %.
Said oils is that heavy crude is or/and treated oil; Wherein heavy crude is selected from one or more in viscous crude, special viscous crude, the ultra viscous crude, and treated oil is selected from one or more in residual oil, catalytically cracked oil, fluid catalytic cracking decant oil, hydrogenation tail oil, oil fuel, solvent treatment extraction oil, wax tailings, deasphalted oil, steam cracking tar, coal tar, the shale oil.20 ℃ of density of said heavy crude are 900～1100kg/m
3Be preferably greater than 950kg/m
3Said oil fuel is selected from 4
#Oil fuel, 5
#Oil fuel, 6
#Oil fuel, 7
#In the oil fuel one or more; Said residual oil is that vacuum residuum is or/and long residuum.
Described viscous crude is that density is 0.90～0.92g/cm
3The crude oil of (20 ℃), described special viscous crude are that density is 0.92～0.98g/cm
3The crude oil of (20 ℃), described ultra viscous crude are that density is greater than 0.98g/cm
3The crude oil of (20 ℃).
The weight ratio of said coal and oils is 0.1～2.0: 1 preferred 0.5～1.0: 1.
Said coker is that delayed coking unit is or/and fluid coker.Preferred 490～510 ℃ of the temperature of pyrogenic reaction.
Description of drawings
Fig. 1 is the principle process synoptic diagram of technical scheme of the present invention.
Fig. 2 is the process flow diagram of embodiment of the present invention.
Embodiment
Two kinds of embodiments of the present invention are described below, but the present invention is not limited to this embodiment.
A kind of method from coal oil-gas reservoir direct production liquid hydrocarbon, this method comprises:
(1), with coal dust broken be particle 100～400 purpose coal dusts;
(2), step (1) gained coal dust and oils are mixed, disperse under 80～300 ℃ and be partly dissolved 3～72 hours after obtain coal oil mixture;
(3), step (2) gained coal oil mixture after process furnace is heated to 480～510 ℃, get in the coke drum and carry out pyrogenic reaction, obtain coke, liquid hydrocarbon and gas.
Said coal is a humic coal or/and sapropelinite, and wherein humic coal is brown coal or/and bituminous coal, bituminous coal be selected from long-flame coal, in the sticking coal, weakly caking coal one or more, sapropelinite is selected from one or more in algal coal, moss coal, the cannel coal.Preferred coal is brown coal, in the bituminous coal in the humic coal one or more in sapropelinite, the humic coal.
The volatile matter of said coal is greater than 30 heavy %.
Said oils is that heavy crude is or/and treated oil; Wherein heavy crude is selected from one or more in viscous crude, special viscous crude, the ultra viscous crude, and treated oil is selected from one or more in residual oil, catalytically cracked oil, fluid catalytic cracking decant oil, hydrogenation tail oil, oil fuel, solvent treatment extraction oil, wax tailings, deasphalted oil, steam cracking tar, coal tar, the shale oil.20 ℃ of density of said heavy crude are 900～1100kg/m
3Be preferably greater than 950kg/m
3Said oil fuel is selected from 4
#Oil fuel, 5
#Oil fuel, 6
#Oil fuel, 7
#In the oil fuel one or more; Said residual oil is that vacuum residuum is or/and long residuum.
The weight ratio of said coal and oils is 0.1～2.0: 1 preferred 0.5～1.0: 1.
The dispersion of step (2) and be partly dissolved preferred 80～200 ℃ of temperature disperses and preferred 5～24 hours of the time that is partly dissolved.
The furnace temp of step (3) is preferably 490～500 ℃.The coke tower top pressure is 0～0.17MPa (gauge pressure).
Below in conjunction with accompanying drawing method provided by the present invention is further explained; Some exemplary device such as ball mill, mixing tank, slurry tank etc. are also optional in the accompanying drawing replaces with the essentially identical miscellaneous equipment of function; The utility appliance of not drawing in the accompanying drawing such as preheater and accessory such as valve etc., but therefore do not limit the present invention.
Fig. 1 is the principle process synoptic diagram of technical scheme of the present invention.
Coal 1 and oils 2 are added mixing tank 3, mix obtaining coal oil mixture 4, coal oil mixture gets into coker 5, under 480～510 ℃, carries out pyrogenic reaction, obtains coke 6, liquid hydrocarbon 7 and gas 8.
Fig. 2 is the process flow diagram of one of embodiment of the present invention.
Coal 1 is crushed to particle diameter 100～400 purpose coal dusts through ball mill 3; All add mixing tank 4 with oils 2; 30～300 ℃ down dissolving obtain coal oil mixture 5 after 3～72 hours, coal oil mixture gets in the process furnace 11 through pump 9, pipeline 10 successively, be heated to 480～510 ℃ best 490～500 ℃ after; Carry out pyrogenic reaction in one in two coke drums 13 of pipeline 12 entering; The sedimentation of coke that reaction generates is full of coke in this coke drum in coke drum, switch to another empty coke drum operation; With coke 14 full scale clearances in this coke drum (shown in dotted line among the figure), coking oil gas then gets into separation column 16 through pipeline 15 and is fractionated into gas 17, coker gasoline 18, coker gas oil 19, wax tailings 20.
Compared with prior art, advantage of the present invention is following:
1, flow process is simple, and operational condition relaxes, and does not need high-tension apparatus, and facility investment is less;
2, do not need consuming hydrogen, do not use catalyzer, process cost is lower;
3, can obtain the liquid hydrocarbon of higher yields, the yield of liquid hydrocarbon weighs about % up to 50;
4, alleviated the coking of process furnace greatly.
Following embodiment will further explain method provided by the invention, but therefore not limit the present invention.
Test is carried out on the delayed coking middle-scale device.The character of feed coal is listed in table 1, and table 2 has been listed the character of oils.
Embodiment 1
Feed coal A is crushed to particle diameter 100～400 purpose coal dusts and 6
#Oil fuel added mixing tank by weight 0.51: 1; Obtain coal oil mixture in dissolving under 150 ℃ after 12 hours; After coal oil mixture entering process furnace is heated to 490 ℃; Get in the coke drum and carry out pyrogenic reaction, the sedimentation of coke that reaction generates is in coke drum, and coking oil gas then gets into separation column and is fractionated into gas and liquid hydrocarbon.Operational condition and material balance are listed in table 3.
Can find out that from table 3 yield of liquid hydrocarbon reaches 48.5 heavy %.
Feed coal B is crushed to particle diameter 100～400 purpose coal dusts; Added mixing tank by weight 1.94: 1 with ultra viscous crude; Obtain coal oil mixture in dissolving under 285 ℃ after 64 hours, after coal oil mixture entering process furnace is heated to 510 ℃, gets in the coke drum and carry out pyrogenic reaction; The sedimentation of coke that reaction generates is in coke drum, and coking oil gas then gets into separation column and is fractionated into gas and liquid hydrocarbon.Operational condition and material balance are listed in table 3.
Can find out that from table 3 yield of liquid hydrocarbon reaches 33.3 heavy %.
Feed coal C is crushed to particle diameter 100～400 purpose coal dusts; Added mixing tank by weight 1.0: 1 with vacuum residuum; Obtain coal oil mixture in dissolving under 200 ℃ after 24 hours, after coal oil mixture entering process furnace is heated to 500 ℃, gets in the coke drum and carry out pyrogenic reaction; The sedimentation of coke that reaction generates is in coke drum, and coking oil gas then gets into separation column and is fractionated into gas and liquid hydrocarbon.Operational condition and material balance are listed in table 3.
Can find out that from table 3 yield of liquid hydrocarbon reaches 42.0 heavy %.
Feed coal A is crushed to particle diameter 100～400 purpose coal dusts; Added mixing tank by weight 0.3: 1 with coal tar; Obtain coal oil mixture in dissolving under 80 ℃ after 3 hours, after coal oil mixture entering process furnace is heated to 490 ℃, gets in the coke drum and carry out pyrogenic reaction; The sedimentation of coke that reaction generates is in coke drum, and coking oil gas then gets into separation column and is fractionated into gas and liquid hydrocarbon.Operational condition and material balance are listed in table 3.
Can find out that from table 3 yield of liquid hydrocarbon reaches 53.1 heavy %.
Table 1
| The feed coal numbering | A | B | C |
| The feed coal kind | Brown coal | Brown coal | Bituminous coal |
| Technical analysis, heavy % | |||
| Moisture M ad | 1.63 | 12.78 | 4.8 |
| Ash content A d | 9.86 | 10.76 | 12.3 |
| Volatile matter V daf | 49.0 | 45.11 | 36.0 |
| Ultimate analysis, heavy % | |||
| Carbon C daf | 78.23 | 74.81 | 80.54 |
| Hydrogen H daf | 6.04 | 5.22 | 5.45 |
| Oxygen O daf | 14.06 | 17.72 | 13.10 |
| Sulphur S daf | 0.22 | 0.45 | 0.65 |
| Nitrogen N daf | 1.44 | 1.80 | 0.26 |
Annotate:
Ad representes air dried basis;
D representes dry base;
Daf representes dry ash-free basis.
Table 2
| The |
6 #Oil fuel | Ultra viscous crude | Vacuum residuum | Coal tar |
| Density (20 ℃), kg/m 3 | 980 (15℃) | 1004 | 970.8 | 1008 |
| Carbon residue, heavy % | 10.8 | 15.7 | 17.0 | / |
| Flash-point, ℃ | 87 | 114 | 110 | / |
| Pour point, ℃ | -9 | 37 | 31 | / |
| Carbon, heavy % | 86.4 | 85.81 | 85.6 | 84.4 |
| Hydrogen, heavy % | 11.2 | 10.81 | 10.3 | 10.36 |
| Oxygen, heavy % | 0.3 | 1.9 | 0.7 | 4.32 |
| Nitrogen, heavy % | 0.41 | 1.02 | 3.0 | 0.61 |
| Sulphur, heavy % | 2.4 | 0.45 | 0.4 | 0.31 |
| Viscosity, mm 2/s | 0.355 (50℃) | 2997 (80℃) | 282.0 (100℃) | 3.68 (50℃) |
| Water cut, heavy % | 0.4 | 0.5 | Trace | 2.8 |
| Ash content, heavy % | 0.054 | 0.35 | 1.0％ | 0.98 |
Table 3
| The embodiment numbering | 1 | 2 | 3 | 4 |
| The feed coal numbering | A | B | C | A |
| The |
6 #Oil fuel | Ultra viscous crude | Vacuum residuum | Coal tar |
| Coal and oils weight ratio | 0.51 | 1.94 | 1.0 | 0.3 |
| Solvent temperature, ℃ | 150 | 285 | 200 | 80 |
| Dissolution time, |
12 | 64 | 24 | 3 |
| Coking condition | ||||
| Temperature, ℃ | 490 | 510 | 500 | 490 |
| Pressure (gauge pressure), MPa | 0 | 0.17 | 0.14 | 0 |
| Coked material balancing | ||||
| Gas, heavy % | 11.3 | 9.5 | 11 | 10.5 |
| Liquid hydrocarbon, heavy % | 48.5 | 33.3 | 42.0 | 53.1 |
| Coke, heavy % | 36.3 | 53.6 | 43.0 | 32.7 |
| Water, heavy % | 4.0 | 3.5 | 2.3 | 3.7 |
Claims (16)
1. method from coal oil-gas reservoir direct production liquid hydrocarbon; It is characterized in that this method is made up of following steps: coal and oils are mixed obtaining coal oil mixture; Coal oil mixture gets into coker, under 480～510 ℃, carries out pyrogenic reaction, obtains coke, liquid hydrocarbon and gas; Said oils is heavy crude or/and treated oil, and 20 ℃ of density of said heavy crude are 900-1100kg/m
3, said treated oil is selected from one or more in residual oil, catalytically cracked oil, fluid catalytic cracking decant oil, hydrogenation tail oil, oil fuel, solvent treatment extraction oil, wax tailings, deasphalted oil, steam cracking tar, coal tar, the shale oil.
2. according to the method for claim 1; It is characterized in that said coal is that humic coal is or/and sapropelinite; Wherein humic coal is brown coal or/and bituminous coal, bituminous coal be selected from long-flame coal, in the sticking coal, weakly caking coal one or more, sapropelinite is selected from one or more in algal coal, moss coal, the cannel coal.
3. according to the method for claim 1, the volatile matter that it is characterized in that said coal is greater than 30 heavy %.
4. according to the method for claim 1, it is characterized in that said oil fuel is selected from 4
#Oil fuel, 5
#Oil fuel, 6
#Oil fuel, 7
#In the oil fuel one or more.
5. according to the method for claim 1, it is characterized in that said residual oil is that vacuum residuum is or/and long residuum.
6. according to the method for claim 1, the weight ratio that it is characterized in that said coal and oils is 0.1～2.0: 1.
7. according to the method for claim 1, it is characterized in that said coker is delayed coking unit or fluid coker.
8. method from coal oil-gas reservoir direct production liquid hydrocarbon is characterized in that this method is made up of following steps:
(1), with coal dust broken for particle be 100～400 purpose coal dusts;
(2), step (1) gained coal dust and oils are mixed, disperse under 30～300 ℃ and be partly dissolved 3～72 hours after obtain coal oil mixture;
(3), step (2) gained coal oil mixture after process furnace is heated to 480～510 ℃, get in the coking tower and carry out pyrogenic reaction, obtain coke, liquid hydrocarbon and gas;
Wherein, said oils is heavy crude or/and treated oil, and 20 ℃ of density of said heavy crude are 900-1100kg/m
3, said treated oil is selected from one or more in residual oil, catalytically cracked oil, fluid catalytic cracking decant oil, hydrogenation tail oil, oil fuel, solvent treatment extraction oil, wax tailings, deasphalted oil, steam cracking tar, coal tar, the shale oil.
9. according to the method for claim 8; It is characterized in that said coal is that humic coal is or/and sapropelinite; Wherein humic coal is brown coal or/and bituminous coal, bituminous coal be selected from long-flame coal, in the sticking coal, weakly caking coal one or more, sapropelinite is selected from one or more in algal coal, moss coal, the cannel coal.
10. according to the method for claim 8, the volatile matter that it is characterized in that said coal is greater than 30 heavy %.
11., it is characterized in that said oil fuel is selected from 4 according to the method for claim 8
#Oil fuel, 5
#Oil fuel, 6
#Oil fuel, 7
#In the oil fuel one or more.
12., it is characterized in that said residual oil is that vacuum residuum is or/and long residuum according to the method for claim 8.
13. according to the method for claim 8, the weight ratio that it is characterized in that said coal and oils is 0.1～2.0: 1.
14. according to the method for claim 8, the weight ratio that it is characterized in that said coal and oils is 0.5～1.0: 1.
15. according to the method for claim 8, it is characterized in that the dispersion of step (2) and being partly dissolved temperature is 80～200 ℃, disperses and the time of being partly dissolved is 5～24 hours.
16. according to the method for claim 8, the furnace temp that it is characterized in that step (3) is 490～500 ℃.
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|---|---|---|---|---|
| US3870621A (en) * | 1973-07-30 | 1975-03-11 | Exxon Research Engineering Co | Residuum processing |
| 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 |
| US20080072476A1 (en) * | 2006-08-31 | 2008-03-27 | Kennel Elliot B | Process for producing coal liquids and use of coal liquids in liquid fuels |
-
2008
- 2008-06-02 CN CN2008101143030A patent/CN101597507B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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