CN102041015A - Method for preparing liquid fuel from coal petrography oil-gas reservoir - Google Patents
Method for preparing liquid fuel from coal petrography oil-gas reservoir Download PDFInfo
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Abstract
The invention provides a method for preparing a liquid fuel from a coal petrography oil-gas reservoir, which comprises the steps: mixing coal powder with heavy oil, aging, thermally melting and dispersing to obtain oil coal slurry, and performing phase separation on the oil coal slurry to obtain liquid hydrocarbon, sol phase and gel phase, wherein the sol phase is cracked in a hydrogenation way, and the gel phase is coked. The method can obtain the qualified liquid fuel only by simply improving the existing refinery equipment, thereby avoiding the complex reaction process that the coal is directly liquefied and is indirectly liquefied. Therefore, the method realizes the development or the separation of the oil in the coal petrography oil-gas reservoir under the real mitigatory condition, thereby being low in investment cost and operation cost. The residue which is generated by the coal-oil co-treatment is subjected to the coking treatment, thus being good for environment and improving the yield of the liquid fuel.
Description
Technical field
The invention belongs to a kind of method of producing liquid fuel from coal oil-gas reservoir.
Background technology
Coal be organism by growth in certain geological age under suitable geologic media, the inflammable minerals that forms through very long incoalation of years.According to the difference of coal-forming plant, coal can divide two big class, i.e. humic coal and sapropelinite.The former originates from higher plant, and is big at the occurring in nature reserves, and it is wide to distribute; The latter originates from lower plant and planktonic organism, and reserves are few.
No matter being the sedimentary organic matter of Lu Sheng or hydrobiont, all is both to have become the oil also can coal-forming, the difference of growing amount just, coal-forming and become between the hydrocarbon component not completely boundary.Under the perfect condition, sedimentary basin edge organic matter is mainly vitrinite and inertinite, easily forms the coal seam; At the middle part of sedimentary basin, organic matter is mainly sapropel group and chitin group, give birth to easily, discharge hydro carbons, and the strange land accumulates in sandstone or the carbonatite space medium hydrocarbon-bearing pool of formation traditional concept.But, not only be present in sandstone or the carbonatite space medium based on the hydrocarbons of 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 with among the fused miniature reservoir space that is wrapped in mutually between the coal petrography macromolecular mass, or is adsorbed on the surface in coal petrography crack or space.According to the preliminary statistics, in China the oil length in Neozoic group's coal petrography (or volatile producibility) between 25 weight %～70 weight %.So the hydrocarbon resources in our called after " coal petrography oil gas (ore deposit) Tibetan " cannot be ignored.
In fact, people have begun to produce the research of liquid fuel for a long time from coal petrography.Produce liquid fuel with coal at present and mainly contain two approach: DCL/Direct coal liquefaction and ICL for Indirect Coal Liquefaction.Direct liquefaction technology is that coal, solvent and mixture of catalysts are generated product liquid with hydrogen reaction under 400～500 ℃, the condition of 15～30MPa, and used catalyzer has the oxide compound or the halogenide of cobalt, molybdenum, tungsten, tin, iron and lead etc.DCL/Direct coal liquefaction technology mainly contains the Shenhua technology of U.S. H-Coal technology, Japanese NEDOL technology, German IGOR technology and China etc.DCL/Direct coal liquefaction need be carried out under the condition that has hydrogen to exist, and makes the organic polymer thaumatropy in the coal be more low molecular liquid fuel, and this reaction needed high pressure and high temperature are no matter above-mentioned its reaction conditions of the sort of technology and technology all are very harsh.
The ICL for Indirect Coal Liquefaction method can be divided into synthetic gas method and methyl alcohol method, and wherein based on the synthetic gas method, this method is earlier coal gas to be turned to synthetic gas (CO and H
2), synthetic liquid fuel and other Chemicals under catalyst action then.The indirect liquefaction technique functions of coal comes from Germany, be German imperial coal research Fischer and Tropsch invent, so it is synthetic to be called as F-T (fischer-tropsch).Probably be at first with the gasification preparing synthetic gas in fact, synthetic gas is adjusted H through purifying
2/ CO ratio synthesizes liquid fuel through F-T catalysis again.The advantage of the indirect liquefaction of coal is the adaptability broad of coal, and operational condition is gentle relatively.During the World War II Germany built together 9 the cover production equipments.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, its total efficiency has only South Africa to have the factory of the ICL for Indirect Coal Liquefaction of scale the biggest in the world not as the direct liquefaction height at present.Therefore, ICL for Indirect Coal Liquefaction method operational path is long, and gordian technique is many, performance difficulty.
For the utilization ratio that improves hydrogen, the quality and the productive rate of oil product, reduce production costs, research and develop coal-oily co-processing technology both at home and abroad.Coal-oily co-processing technology is actually over the DCL/Direct coal liquefaction technology developed and the combination of slag oil crack technology.Coal, residual oil and catalyzer are produced liquid fuel under the effect of high pressure hydrogen.But technology in the past is isolated often for the selection of heavy oil and coal, simultaneously, residue is lacked good treatment process, and therefore the effect of reaction is not satisfactory.
Summary of the invention
Technical problem to be solved by this invention is to handle the residue that produces in coal-oily co-processing technology, improves the productive rate of liquid fuel.
The objective of the invention is on the basis of above-mentioned discovery, to provide a kind of method of producing liquid fuel from coal oil-gas reservoir.
Technical scheme the following step of the present invention:
(1) with coal dust broken be 100～200 purpose coal dusts;
(2) coal dust, heavy oil are mixed, ageing obtains coal oil mixture;
(3) coal oil mixture and solubility promoter mix, and enter the thermosol device and carry out thermosol, dispersion;
(4) thermosol, the slurries after disperseing enter phase-separating device and are separated, and obtain liquid hydrocarbon, colloidal sol mutually and gel phase;
(5) colloidal sol enters the hydrocracking device mutually, obtains hydrogenation gas, hydrogenation distillate and hydrogenated residue;
(6) gel phase and hydrogenated residue enter coker, obtain coking gas, coking oil and coke.
Described 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 V of described coal
DafBe 35～60 heavy % (daf represents dry ash-free basis), carbon atom is 65～85 heavy %, and hydrogen atom is 4～8 heavy %.
Described heavy oil is heavy crude, is selected from viscous crude, special viscous crude, the super viscous crude one or more, and 20 ℃ of density of described heavy crude are 900～1100kg/m
3Be preferably greater than 950kg/m
3Described viscous crude is that density is 900～920kg/m
3The crude oil of (20 ℃), described special viscous crude are that density is 920～980kg/m
3The crude oil of (20 ℃), described super viscous crude are that density is greater than 980kg/m
3The crude oil of (20 ℃).
Preferred coal is identical with the geological age of heavy oil birth.The weight ratio of described coal and heavy oil is 0.1～1.5: 1 preferred 0.5～1.0: 1.
Coal dust and heavy oil blended temperature are 40～80 ℃, and stirring velocity is 100～200 rev/mins, and churning time is 30～60 minutes, and ageing dissolved it in 1～48 hour more fully then.
Described solubility promoter is a kind of help coal dissolved anion surfactant, has hydrophilic and lipophilic performance, and has dispersion, solubilising, infiltration and function such as wetting.Preferred solubility promoter is 1,4-two (2-ethylhexyl) succinate sulfonate, and it is the sulfonate of the esterification products of MALEIC ANHYDRIDE and 2-Ethylhexyl Alcohol.Its chemical structural formula is:
Wherein M is basic metal such as Na, K etc.
Described solubility promoter accounts for 0.1～2 heavy % of coal oil mixture total amount.
Coal oil mixture after the ageing and solubility promoter mix, and enter the thermosol device and carry out thermosol, dispersion.Described thermosol device is the thermosol Scattered Kettle that has water distilling apparatus, and stirring velocity is 100～300 rev/mins, and temperature is 120～200 ℃, and the time is 1～12 hour.
Slurries are put into phase-separating device then, in temperature are to be separated under 120～200 ℃ the condition.Described phase-separating device is a slurry tank, and liquid hydrocarbon is extracted out from the slurry tank top, and hydrogen-rich colloidal sol is extracted out from slurry tank top, and the gel phase of poor hydrogen is extracted out from the slurry tank bottom.Colloidal sol is to be formed by the colloidal particles of coal and solvent mutually, and gel phase is formed by the macrobead of coal and solvent.
Described colloidal sol enters the hydrocracking device mutually, contacts with hydrocracking catalyst, and the hydrocracking reaction conditions is: hydrogen dividing potential drop 2～30MPa, 400～450 ℃ of temperature.Hydrocracking obtains hydrogenation gas, hydrogenation distillate and hydrogenated residue.Hydrocracking catalyst is the sulfomethylated lignin acid metal complex, the complex compound that forms by transition metal and lignosulfonic acid, wherein transition metal is selected from the iron group of group VIII or/and the chromium sub-group element of group vib, in iron group chosen from Fe, cobalt, the nickel one or more, chromium sub-group element are selected from one or more in chromium, molybdenum, the tungsten.Hydrocracking catalyst accounts for 1～2 heavy % of colloidal sol phase.
Described gel phase then enters coker.Described coker is that delayed coking unit is or/and fluid coker.Preferred 490～510 ℃ of the temperature of pyrogenic reaction.
Preferably, liquid hydrocarbon, hydrogenation distillate and the coking oil that obtains that is separated enters hydro-refining unit, obtains qualified gasoline, kerosene and diesel oil, and hydro-refining unit is the hydro-refining unit of conventional refinery.
Preferably, coking gas is sent into hydrogen generating system and is obtained hydrogen, and hydrogen can be used as above-mentioned hydrocracking device or/and the hydrogen source of hydro-refining unit.
The water that whole technology obtains enters Sewage treatment systems.
Advantage of the present invention:
(1) the present invention has made full use of the similarity of coal and heavy crude, make coal under the assistance of solubility promoter as much as possible thermosol be scattered among the heavy crude, form the colloidal sol phase, thereby can use existing mink cell focus hydrocracking device, thereby simplify the technology of coal system oil greatly;
(2) avoided the complex reaction process of DCL/Direct coal liquefaction and indirect liquefaction, but realized the exploitation or the separation of oil gas in the coal oil-gas reservoir under real demulcent condition, cost of investment and running cost are all lower;
(3) because colloidal sol phase and the gel phase made with the present invention can both enlarge existing refining process unit raw material sources with the processing of existing refining process unit, improved the value of coal again;
(4) handle the residue that produces in coal-oily co-processing technology by coking, both be beneficial to environment, improve the productive rate of liquid fuel simultaneously again.
Description of drawings
Fig. 1 is the principle process synoptic diagram of technical solution of the present invention.
Fig. 2 is the principle process synoptic diagram of optimal technical scheme of the present invention.
Embodiment
Below in conjunction with accompanying drawing method provided by the present invention is given further instruction, but not thereby limiting the invention.
Fig. 1 is the principle process synoptic diagram of technical solution of the present invention.
The principle process of technical solution of the present invention is as follows:
Particle diameter 100～200 purpose coal dusts, heavy oil obtain coal oil mixture through pipeline 1 and 2 mixing, ageing respectively, coal oil mixture and solubility promoter mix, enter thermosol device 3 and carry out thermosol, dispersion, slurries after thermosol, the dispersion enter phase-separating device 5 through pipeline 4 and are separated, obtain liquid hydrocarbon, colloidal sol phase and gel phase, draw through pipeline 6,7,8 respectively.Wherein colloidal sol enters hydrocracking device 9 through pipeline 7, contacts with hydrocracking catalyst, and hydrocracking obtains hydrogenation gas, hydrogenation distillate and hydrogenated residue, draws through pipeline 10,11,12 respectively.Gel phase, hydrogenated residue enter coker 13 through pipeline 8,12 respectively, carry out pyrogenic reaction under 480～510 ℃, obtain coking gas, coking oil and coke, draw through pipeline 14,15,16 respectively.
Fig. 2 is the principle process synoptic diagram of optimal technical scheme of the present invention.
The principle process of optimal technical scheme of the present invention is as follows:
Particle diameter 100～200 purpose coal dusts, heavy oil mix through pipeline 1 and 2 respectively, ageing obtains coal oil mixture, coal oil mixture and solubility promoter mix, enter thermosol device 3 and carry out thermosol, dispersion, slurries after thermosol, the dispersion enter phase-separating device 5 through pipeline 4 and are separated, obtain liquid hydrocarbon, colloidal sol phase and gel phase, draw through pipeline 6,7,8 respectively.Wherein colloidal sol enters hydrocracking device 9 through pipeline 7, contacts with hydrocracking catalyst, and hydrocracking obtains hydrogenation gas, hydrogenation distillate and hydrogenated residue, draws through pipeline 10,11,12 respectively.Gel phase, hydrogenated residue enter coker 13 through pipeline 8,12 respectively, carry out pyrogenic reaction under 480～510 ℃, obtain coking gas, coking oil and coke, draw through pipeline 14,15,16 respectively.Be separated the liquid hydrocarbon, hydrogenation distillate and the coking oil content that obtain not after pipeline 6,11,15 mixes, enter hydro-refining unit 18, obtain qualified gasoline, kerosene and diesel oil and draw through pipeline 19,20,21 respectively through pipeline 17.Coking gas is sent into hydrogen generating system 22 through pipeline 14 and is obtained hydrogen, hydrogen through pipeline 23 draw or as above-mentioned hydrocracking device 9 or/and the hydrogen source of hydro-refining unit 18.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
The character of feed coal is listed in table 1, and table 2 has been listed heavy crude and colloidal sol viscosity mutually.
Example 1 thermosol and dispersion
(20 ℃ of density are 950kg/m to get the natural heavy crude of 1kg Shengli Oil Field
3, the H/C mol ratio is 1.61) and Huangxian county, 0.6kg Shandong brown coal.Coal dust is broken into coal dust, 100～200 orders.Huangxian county coal is created on husky three sections of the Tr, and is the same with the natural heavy crude of Shengli Oil Field, also is husky three sections of the Tr, and its character sees Table 1.
The technical analysis and the element data of table 1, Huangxian county, Shandong brown coal
| Technical analysis | Ultimate analysis |
| Moisture M ad, heavy %9.55 | C, heavy %77.39 |
| Ash content A d, heavy %11.86 | H, heavy %5.53 |
| Volatile matter V daf, heavy %45.11 | N, heavy %2.14 |
| S, heavy %0.77 | |
| O, heavy %14.17 |
After mix stirring, ageing 24 hours adds the solubility promoter 1 of 0.5 heavy %, behind 4-two (2-ethylhexyl) the succinate sodium sulfonate, in the time of 80 ℃, fully stir stirring velocity～150 rev/min, enter the thermosol Scattered Kettle then, under 130 ℃ situation, constantly stir with 200 rev/mins speed, put into slurry tank after 4 hours, keep 150 ℃ of temperature, quiescent settling, the top colloidal sol 1.249kg that makes an appointment, bottom gel phase 0.23kg is in the thermosol dispersion process, obtain water 103 grams, liquid hydrocarbon 18 grams.That is to say that nearly 45% coal is dissolved or dispersed among the crude oil.The scanning electron microscope analysis result shows the colloidal solid that has many 10～200nm during colloidal sol mutually, so we are called the colloidal sol phase, and the granular size in the gel phase is just high-visible under biomicroscope, all in the micron number magnitude.Because colloidal sol has dissolved the part coal in mutually, there is the part colloidal solid to be scattered in wherein again simultaneously, so its viscosity ratio heavy crude has increased (seeing Table 2) greatly.
Table 2 heavy crude and colloidal sol viscosity (mm mutually
2/ s, 100 ℃)
| The natural heavy crude of Shengli Oil Field | Colloidal sol phase (oil/coal=1/0.6) |
| 2.0 | 6.8 |
The hydrocracking of example 2 colloidal sol phases
Use JQ-100 heavy-oil hydrogenation high-pressure micro-device.The hydrocracking catalyst that uses is iron-chromium lignin sulfonic acid (FeCr-LS), and hydrocracking catalyst accounts for 1.5 heavy % of colloidal sol phase.The M of colloidal sol phase
Ad≤ 0.1 heavy %, A
Ad≤ 0.2 heavy %, H/C=1.52 (mol ratio), O/C=0.048, density (20 ℃)=1050kg/m
3430 ℃ of reactant temperature outs, initial hydrogen dividing potential drop 5.6MPa.The density of hydrogenation distillate (20 ℃)=900kg/m as a result
3, H/C brings up to 1.78, its A
Ad≤ 0.05%.The H/C=1.28 of hydrogenated residue (mol ratio).
The pyrogenic reaction of example 3 gel phases and hydrogenated residue
Coking test is carried out on the delayed coking middle-scale device.Coal oil mixture enters process furnace, be heated to 490 ℃ after, enter and carry out pyrogenic reaction in the coke drum, the sedimentation of coke that reaction generates is in coke drum, coking oil gas then enters separation column and is fractionated into coking gas and coking oil.Operational condition and material balance are listed in table 3, and the boiling range of coking oil is listed in table 4, and the coke nature tabular is in table 5.
Table 3 coking operation condition and material balance
| The coking operation condition | |
| Temperature, ℃ | 490 |
| Pressure (gauge pressure), MPa | 0 |
| Coked material balancing | |
| Coking gas, heavy % | 7.5 |
| Coking oil, heavy % | 37.5 |
| Coke, heavy % | 51.3 |
| Water, heavy % | 3.7 |
The boiling range of table 4 coking oil
Table 5 coke property
| Volatile matter V daf/ heavy % | Moisture M ad/ heavy % | Ash content A ad/ heavy % | Calorific value/(kcal/g) |
| 12.7 | - | 11.21 | 8300 |
Annotate:
Ad represents air dried basis;
D represents dry base;
Daf represents dry ash-free basis;
IBP represents initial boiling point;
FBP represents final boiling point.
Claims (17)
1. produce the method for liquid fuel from coal oil-gas reservoir for one kind, it is characterized in that this method comprises the following steps:
(1) with coal dust broken be 100～200 purpose coal dusts;
(2) coal dust, heavy oil are mixed, ageing obtains coal oil mixture;
(3) coal oil mixture and solubility promoter mix, and enter the thermosol device and carry out thermosol, dispersion;
(4) thermosol, the slurries after disperseing enter phase-separating device and are separated, and obtain liquid hydrocarbon, colloidal sol mutually and gel phase;
(5) colloidal sol enters the hydrocracking device mutually, obtains hydrogenation gas, hydrogenation distillate and hydrogenated residue;
(6) gel phase and hydrogenated residue enter coker, obtain coking gas, coking oil and coke.
2. according to the method for claim 1, it is characterized in that described 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 or 2, it is characterized in that the volatilization of described coal is divided into 35～60 heavy %, carbon atom is 65～85 heavy %, and hydrogen atom is 4～8 heavy %.
4. according to the method for claim 1, it is characterized in that described heavy oil is heavy crude, be selected from viscous crude, special viscous crude, the super viscous crude one or more.
5. according to the method for claim 4, it is characterized in that 20 ℃ of density of described heavy crude are 900～1100kg/m
3
6. according to the method for claim 1, it is characterized in that described coal is identical with the geological age of heavy oil birth.
7. according to the method for claim 1, the weight ratio that it is characterized in that described coal and heavy oil is 0.1～1.5: 1.
8. according to the method for claim 1, it is characterized in that described coal dust and heavy oil blended temperature are 40～80 ℃, stirring velocity is 100～200 rev/mins, and churning time is 30～60 minutes, and ageing is 1～48 hour then.
9. according to the method for claim 1, it is characterized in that described solubility promoter is 1,4-two (2-ethylhexyl) succinate sulfonate.
10. according to the method for claim 1, it is characterized in that described solubility promoter accounts for 0.1～2 heavy % of coal oil mixture total amount.
11. according to the method for claim 1, it is characterized in that described thermosol device is the thermosol Scattered Kettle that has water distilling apparatus, stirring velocity is 100～300 rev/mins, temperature is 120～200 ℃, and the time is 1～12 hour.
12., it is characterized in that described colloidal sol enters the hydrocracking device mutually according to the method for claim 1, contact with hydrocracking catalyst, the hydrocracking reaction conditions is hydrogen dividing potential drop 2～30MPa, 400～450 ℃ of temperature.
13. method according to claim 12, it is characterized in that described hydrocracking catalyst is the sulfomethylated lignin acid metal complex, the complex compound that forms by transition metal and lignosulfonic acid, wherein transition metal is selected from the iron group of group VIII or/and the chromium sub-group element of group vib, in iron group chosen from Fe, cobalt, the nickel one or more, chromium sub-group element are selected from one or more in chromium, molybdenum, the tungsten.
14., it is characterized in that described hydrocracking catalyst accounts for 1～2 heavy % of colloidal sol phase according to the method for claim 12.
15. according to the method for claim 1, it is characterized in that described coker is a delayed coking unit or/and fluid coker, the temperature of pyrogenic reaction is 490～510 ℃.
16., it is characterized in that described liquid hydrocarbon, hydrogenation distillate and the coking oil that obtains that is separated enters hydro-refining unit, obtains qualified gasoline, kerosene and diesel oil according to the method for claim 1.
17., it is characterized in that described coking gas sends into hydrogen generating system and obtain hydrogen according to the method for claim 1.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106170533A (en) * | 2013-12-20 | 2016-11-30 | 全球网关卢森堡控股有限公司 | Produce the method for combustion gas by carbonaceous material |
| CN110144249A (en) * | 2019-05-16 | 2019-08-20 | 煤炭科学技术研究院有限公司 | The preparation method of high matching coal |
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| CN1236806A (en) * | 1999-03-03 | 1999-12-01 | 苏宏文 | Oil-water-coal slurry and its preparing process |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106170533A (en) * | 2013-12-20 | 2016-11-30 | 全球网关卢森堡控股有限公司 | Produce the method for combustion gas by carbonaceous material |
| CN110144249A (en) * | 2019-05-16 | 2019-08-20 | 煤炭科学技术研究院有限公司 | The preparation method of high matching coal |
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Effective date of registration: 20110602 Address after: 100029 Beijing city Chaoyang District huixinxijie Lanjue court 3-1202 Applicant after: Jin Jun Co-applicant after: Niu Jiayu Co-applicant after: Wang Haoping Co-applicant after: Hou Chuangye Address before: 100029 Beijing city Chaoyang District huixinxijie Lanjue court 3-1202 Applicant before: Jin Jun Co-applicant before: Niu Jiayu Co-applicant before: Wang Haoping Co-applicant before: Hou Chuangye Co-applicant before: Yang Yuanyi |
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Application publication date: 20110504 |
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