CN106147889B - A kind of method of coal clean fuel and the high-octane gasoline and modification diesel oil obtained with this method - Google Patents
A kind of method of coal clean fuel and the high-octane gasoline and modification diesel oil obtained with this method Download PDFInfo
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- CN106147889B CN106147889B CN201510182110.9A CN201510182110A CN106147889B CN 106147889 B CN106147889 B CN 106147889B CN 201510182110 A CN201510182110 A CN 201510182110A CN 106147889 B CN106147889 B CN 106147889B
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- 238000000034 method Methods 0.000 title claims abstract description 65
- 239000003245 coal Substances 0.000 title claims abstract description 61
- 239000003502 gasoline Substances 0.000 title claims abstract description 37
- 239000002283 diesel fuel Substances 0.000 title claims abstract description 36
- 239000000446 fuel Substances 0.000 title claims abstract description 28
- 230000004048 modification Effects 0.000 title claims description 7
- 238000012986 modification Methods 0.000 title claims description 7
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 195
- 239000007789 gas Substances 0.000 claims abstract description 76
- 239000001257 hydrogen Substances 0.000 claims abstract description 73
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 73
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 67
- 239000011280 coal tar Substances 0.000 claims abstract description 34
- 238000002309 gasification Methods 0.000 claims abstract description 29
- 239000003034 coal gas Substances 0.000 claims abstract description 26
- 238000000197 pyrolysis Methods 0.000 claims abstract description 21
- 238000006266 etherification reaction Methods 0.000 claims abstract description 20
- 230000008569 process Effects 0.000 claims abstract description 20
- 238000010926 purge Methods 0.000 claims abstract description 18
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 238000004821 distillation Methods 0.000 claims abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims description 60
- 238000003786 synthesis reaction Methods 0.000 claims description 42
- 239000012530 fluid Substances 0.000 claims description 31
- 239000003054 catalyst Substances 0.000 claims description 28
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 21
- 230000015572 biosynthetic process Effects 0.000 claims description 16
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 12
- 229910052681 coesite Inorganic materials 0.000 claims description 11
- 229910052593 corundum Inorganic materials 0.000 claims description 11
- 229910052906 cristobalite Inorganic materials 0.000 claims description 11
- 238000005194 fractionation Methods 0.000 claims description 11
- 239000000377 silicon dioxide Substances 0.000 claims description 11
- 229910052682 stishovite Inorganic materials 0.000 claims description 11
- 229910052905 tridymite Inorganic materials 0.000 claims description 11
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 11
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 10
- 230000008859 change Effects 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 7
- 239000002131 composite material Substances 0.000 claims description 6
- 238000001179 sorption measurement Methods 0.000 claims description 6
- 238000009835 boiling Methods 0.000 claims description 4
- 238000005336 cracking Methods 0.000 claims description 3
- 239000003377 acid catalyst Substances 0.000 claims description 2
- 238000004508 fractional distillation Methods 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 239000002994 raw material Substances 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 117
- 239000000047 product Substances 0.000 description 34
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 15
- 238000005984 hydrogenation reaction Methods 0.000 description 13
- 239000005864 Sulphur Substances 0.000 description 10
- 229910052751 metal Inorganic materials 0.000 description 9
- 239000002184 metal Substances 0.000 description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 8
- 238000004517 catalytic hydrocracking Methods 0.000 description 8
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 8
- 229910052760 oxygen Inorganic materials 0.000 description 8
- 239000001301 oxygen Substances 0.000 description 8
- 239000004615 ingredient Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 150000002431 hydrogen Chemical class 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 239000000295 fuel oil Substances 0.000 description 5
- 238000009996 mechanical pre-treatment Methods 0.000 description 5
- 229910052717 sulfur Inorganic materials 0.000 description 5
- 239000011593 sulfur Substances 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 239000012528 membrane Substances 0.000 description 4
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 150000002739 metals Chemical class 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000002808 molecular sieve Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000010742 number 1 fuel oil Substances 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000003111 delayed effect Effects 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000006011 modification reaction Methods 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000003348 petrochemical agent Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 238000005292 vacuum distillation Methods 0.000 description 2
- 239000001993 wax Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 239000004642 Polyimide Substances 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910021417 amorphous silicon Inorganic materials 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- 238000005815 base catalysis Methods 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000011286 gas tar Substances 0.000 description 1
- 239000003254 gasoline additive Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- COTNUBDHGSIOTA-UHFFFAOYSA-N meoh methanol Chemical compound OC.OC COTNUBDHGSIOTA-UHFFFAOYSA-N 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 229920002492 poly(sulfone) Polymers 0.000 description 1
- 229920001721 polyimide Polymers 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000007142 ring opening reaction Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Abstract
The invention discloses a kind of methods of coal clean fuel, comprising: by raw material pyrolysis of coal, obtains coal tar, semicoke and pyrolysis coal gas；Semicoke is obtained into gasification raw gas through gasification, methanol is prepared after transformed, obtains methanol and methanol purge gas；Pyrolysis coal gas is mixed with methanol purge gas, hydrogen is mentioned and obtains hydrogen；Coal tar is subjected to distillation separation, obtains carbolic oil fraction and heavy end；Carbolic oil fraction and methanol are subjected to etherification reaction, obtain antiknock component；Heavy end is subjected to hydrofinishing and hydrocracked, treated, product is fractionated and obtains gasoline fraction and diesel oil distillate；Antiknock component and gasoline fraction are reconciled and produce high-octane gasoline；Diesel oil distillate is subjected to hydro-upgrading process for producing and modifies diesel oil.The present invention directly produces the clean fuel of high-quality from feed coal, and the abundant deep processing to coal resources realizes the system connectivity between each production technology, has reached the efficient and clean utilization of coal resources.
Description
Technical field
The present invention relates to coal field of deep, and in particular, to a kind of method of coal clean fuel.
Background technique
China is the country of rich coal resources and petroleum resources relative shortage, with fast-developing China of national economy
Demand to oil product grows continuously and fast, therefore, in order to ensure the sustainable development of Chinese national economy, Optimization of Energy Structure,
The dependence to petroleum import is reduced, China's coal resources advantage abundant is made full use of, greatly develops the production of coal chemical industry new and high technology
Industry has become the inevitable choice of China's energy strategy with coal chemical industry products substitution part petrochemicals.Coal oil
(Coal-to-liquids, CTL) is to produce oil product and petrochemicals by chiral process using coal as raw material
One technology, currently used coal oil technology mainly have the methods of DCL/Direct coal liquefaction and ICL for Indirect Coal Liquefaction.
The direct liquefaction of coal under high-temperature and high-pressure conditions, fires coal by catalytic hydrogenation direct liquefaction synthesizing liquid hydro carbons
Material, and remove the atoms such as sulphur, nitrogen, oxygen.With the type bad adaptability to coal, reaction and operating condition are harsh, output fuel oil
The impurity contents such as aromatic hydrocarbons, sulphur and nitrogen are high, the low feature of Cetane number, directly use more difficulty, oil product on the engine and are not inconsistent
It closes national standard (GB 19147-2009).
The indirect liquefaction of coal is converted into HC fuel first coal gasification, then by F- T synthesis.Oil product sulphur, the nitrogen of production
Content is low, but the indexs such as Cetane number of oil product do not meet national standard still.
And coal first passes through pyrolytic process and obtains coal tar, then coal tar is carried out hydrotreating to produce liquid fuel (such as
Diesel oil) technology be increasingly taken seriously.
CN101643654A discloses the processing technology of a kind of non-caking coal or weak caking coal.Non-caking coal is weak
Low temperature distillation reaction, generates coal gas, semicoke and coal tar in binding coal progress；By pressure-variable adsorption by the hydrogen in the coal gas
Air lift goes out；The semicoke is sent into gas producer, semicoke, oxygen and vapor reaction generate synthesis gas in gas producer
And coal ash, the synthesis gas include carbon monoxide and hydrogen；Or semicoke feeding circulating fluidized bed boiler is generated electricity；
The coal tar is subjected to normal pressure fractionation, obtains light fraction, carbolic oil and bottom of tower heavy oil, bottom of tower heavy oil is dragged by vacuum fractionation removing
Tail pitch obtains heavy distillat；Carbolic oil carries out carbolic oil and extracts to obtain phenols and dephenolize oil；By light fraction, dephenolize oil and heavy distillat, with
Hydrogen carries out hydrogenation reaction.
102816596 A of CN discloses the deep working method of a kind of non-caking coal or weak caking coal.By incoherence
Low temperature distillation reaction in coal or weak caking coal progress, generates coal gas, semicoke and coal tar；It will be described by pressure swing absorption process
Hydrogen in coal gas is separated, and obtained hydrogen is used for hydrogenation process；Semicoke generates synthesis gas in gas producer, closes
F-T synthesis reaction, which is carried out, at gas produces paraffin class hydro carbons；The oil gas and be hydrocracked that tar stock, delayed coking reaction obtain
Liquid product enters destilling tower jointly, distills out naphtha cut, carbolic oil fraction, wax oil fraction and tower bottom oil；Naphtha evaporates
Divide and is mixed into petroleum naphtha hydrogenation refining reaction section with hydrogen；The dephenolize oil and wax oil fraction that carbolic oil fraction obtains after dephenolize
It is mixed into hydrotreating reaction section；The fractionation of hydrotreating reaction liquid phase is light fraction and heavy distillat, and heavy distillat carries out plus hydrogen is split
Change；It distills obtained tower bottom oil and enters delayed coking unit
103160305 A of CN discloses a kind of system and technique that fuel oil is directly prepared using coal.Firstly, feed coal
It is pyrolyzed in pyrolysis oven, generates coal gas, coal tar and semicoke；Semicoke is converted into gasification raw gas and coal tar by gasification furnace
Oil；Raw gas is separated and washing obtains synthesis gas, and synthesis gas carries out F- T synthesis diesel oil；Coal gas will be pyrolyzed using pressure-variable adsorption
Middle Hydrogen Separation comes out；Gasification coal tar and pyrolysis coal tar are mixed to get mixed coal tar, using the hydrogen of extracting to mixing
Coal tar carries out hydrofinishing processing, obtains coal tar hydrogenating diesel oil, then, deploys to obtain high-quality bavin with F- T synthesis diesel oil
Oil.
But the above-mentioned prior art is still not perfect the processing technology of coal tar, obtained oil product is unable to reach national mark
Standard, therefore oil product made from coal tar needs and petrochemical industry oil product mixture, and the indexs such as the Cetane number of final oil product can be made to accord with
Close national standard.
Therefore, coal resources can be converted to there is an urgent need to develop one kind the combustion for meeting the even higher standard requirements of national standard
The process of material.
Summary of the invention
In order to overcome the disadvantage of oil product difference existing for existing coal oil technique, coal resources can be converted to by providing one kind
Meet the process of the clean fuel of the even higher standard requirements of national standard, this method comprises:
(1) under the conditions of 450-650 DEG C, feed coal is pyrolyzed, obtains coal tar, semicoke and pyrolysis coal gas；
(2) semicoke that step (1) obtains is obtained into gasification raw gas through gasification, carries out methanol synthesis reaction after transformed,
Obtain methanol and methanol purge gas；
(3) the pyrolysis coal gas that step (1) obtains is mixed with the methanol purge gas that step (2) obtains, and is mentioning hydrogen condition
Under, obtain hydrogen；
(4) under conditions of 190-220 DEG C, the coal tar that step (1) obtains is subjected to distillation separation, obtains carbolic oil fraction
And heavy end；
(5) the carbolic oil fraction that step (4) obtains and the methanol that step (2) obtain are subjected to etherification reaction, obtain higher octane
It is worth component；
(6) heavy end for obtaining step (4) carries out hydrofinishing, and refined products are fractionated and obtain gasoline fraction, bavin
Oil distillate and tail oil fraction；
(7) antiknock component that step (5) obtains is reconciled with obtained gasoline fraction is fractionated in step (6),
High-octane gasoline is made；
(8) diesel oil distillate is subjected to hydro-upgrading processing, modification diesel oil is made；
(9) at least part hydrogen that step (3) obtains is passed through the hydrofinishing of step (6) and/or adding for step (8)
In hydrogen modification reaction.
Another aspect provides high-octane gasoline of the method acquisition by the coal clean fuel
With modification diesel oil.
The method of coal clean fuel provided by the invention realizes the abundant deep processing to coal resources, obtains Gaoxin
Alkane value component, produces the clean fuel of high-quality, while realizing the system connectivity between each production technology, improves system
Efficiency maximizes utilizing for the energy, has reached the efficient and clean utilization of coal resources.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
Fig. 1 is the schematic diagram of process flow in the embodiment of the present invention 1；
Fig. 2 is the schematic diagram of process flow in the embodiment of the present invention 2；
Fig. 3 is the schematic diagram of another embodiment of the present invention.
Specific embodiment
Below in conjunction with attached drawing, detailed description of the preferred embodiments.It should be understood that this place is retouched
The specific embodiment stated is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
The present invention provides a kind of methods of coal clean fuel, wherein this method comprises:
(1) under the conditions of 450-650 DEG C, feed coal is pyrolyzed, obtains coal tar, semicoke and pyrolysis coal gas；
(2) semicoke that step (1) obtains is obtained into gasification raw gas through gasification, carries out methanol synthesis reaction after transformed,
Obtain methanol and methanol purge gas；
(3) the pyrolysis coal gas that step (1) obtains is mixed with the methanol purge gas that step (2) obtains, and is mentioning hydrogen condition
Under, obtain hydrogen；
(4) under conditions of 190-220 DEG C, the coal tar that step (1) obtains is subjected to distillation separation, obtains carbolic oil fraction
And heavy end；
(5) the carbolic oil fraction that step (4) obtains and the methanol that step (2) obtain are subjected to etherification reaction, obtain higher octane
It is worth component；
(6) heavy end for obtaining step (4) carries out hydrofinishing, and refined products are fractionated and obtain gasoline fraction, bavin
Oil distillate and tail oil fraction；
(7) antiknock component that step (5) obtains is reconciled with obtained gasoline fraction is fractionated in step (6),
High-octane gasoline is made；
(8) diesel oil distillate is subjected to hydro-upgrading processing, modification diesel oil is made；
(9) at least part hydrogen that step (3) obtains is passed through the hydrofinishing of step (6) and/or adding for step (8)
In hydrogen modification reaction.
In the present invention, the tail oil that step (6) obtains belongs to heavy end, can be hydrocracked to it, it is therefore preferable that
In the case of, the method for coal clean fuel provided by the invention further include: the tail oil fraction that step (6) obtains is carried out plus hydrogen is split
Change, in the refined products that crackate is incorporated to the heavy end that step (4) obtains and/or step (6) obtains, and then realization pair
The effective use of heavy end.
The optional range of condition being hydrocracked is larger, and under preferable case, the condition being hydrocracked may include:
Cracking temperature can be 360-400 DEG C, and pressure can be 8-20MPa, and hydrogen to oil volume ratio can be 800-2000:1, Mean fluid
Air speed can be 0.5h-1-3h-1。
According to the present invention, the hydrocracking reaction preferably carries out in the presence of a catalyst, and the catalyst is not specific
It limits, can be the conventional selection of this field, hydrocracking process used catalyst is conventional hydrocracking catalyst, mainly
Using group VIB and group VIII metal as active component, using amorphous silicon aluminium and molecular sieve as carrier, vib metals are general
For Mo and/or W, group VIII metal Co and/or Ni.
In the present invention, for the quality of the diesel component further improved, coal system cleaning combustion provided by the invention
The diesel component that the method for material also obtains step (6) carries out hydro-upgrading, and the condition of the hydro-upgrading can be in very big model
Enclose interior change, under preferable case, the condition of the hydro-upgrading include: reaction temperature be 360-400 DEG C, pressure 8-20MPa,
Hydrogen to oil volume ratio is 500-2000:1 (preferably, hydrogen to oil volume ratio 800-2000:1), and Mean fluid air speed is 0.5h-1-3h-1.It is highly preferred that it is 380-400 DEG C, pressure 10-20MPa that the condition of the hydro-upgrading, which includes: reaction temperature, hydrogen oil volume
Than for 1000-2000:1, Mean fluid air speed is 0.5h-1-1.5h-1。
According to the present invention, the hydro-upgrading reaction preferably carries out in the presence of a catalyst, and the catalyst is not specific
It limits, can be the conventional selection of this field, the catalyst is to urge with what higher selectivity of ring-opening and good aromatic hydrocarbons were saturated
Agent, mainly using group VIB and group VIII metal as active component, vib metals are generally Mo and/or W, group VIII
Metal Co and/or Ni, using salic, silicon-containing alumina and molecular sieve as carrier.
According to the present invention, in step (2), the condition of the gasification can change in very large range, under preferable case, institute
It is 0.07-3MPa that the condition for stating gasification, which may include: vapor pressure, and gasification temperature is 1000-1200 DEG C.It is highly preferred that described
The condition of gasification includes: that vapor pressure is 0.1-3MPa, and gasification temperature is 1000-1200 DEG C.
In the present invention, in step (2), reactor, reaction condition and the catalyst of the methanol synthesis reaction can roots
It is selected and is adjusted according to actual needs, under preferable case, the methanol synthesis reaction is carried out on fixed bed reactors, institute
It is 220-280 DEG C, pressure 5-10MPa that the condition for stating methanol synthesis reaction, which includes: temperature, and synthesis gas air speed is 4000-
10000h-1.It is highly preferred that it is 260-280 DEG C, pressure 5-7MPa that the condition of the methanol synthesis reaction, which includes: temperature, synthesis
Gas air speed is 4000-6000h-1；The catalyst of the methanol synthesis reaction can be CuO/ZnO/Al2O3Catalyst.
In the present invention, in step (3), the method for mentioning hydrogen can for it is well known in the art it is various mention hydrogen methods, preferably
In the case of, the method for mentioning hydrogen is pressure swing adsorption method, and the condition of pressure swing adsorption method includes: that pressure is 0.3-4.0MPa, absorption
Agent is selected from least one of aluminium oxide, silica gel, active carbon and zeolite molecular sieve, as shown in Figure 3.Optionally, in step (3),
The method for mentioning hydrogen may be membrane separation process, and the pressure of membrane separation process as depicted in figs. 1 and 2 is 0.3-2.0MPa, described
The type of film used in membrane separation process is known to those skilled in the art, such as can be by being selected from polyimides and polysulfones high score
Sub- polymer is made.
According to the present invention, in the etherification reaction of step (5), phenol in carbolic oil fraction and the molar ratio of methanol can be 1:
1-5；Preferably 1:3-5.The condition of the etherification reaction can change in very large range, it is preferable that the etherification reaction
Condition may include that temperature is 350-450 DEG C, and the molar ratio of phenol and alcohol is 1:1-5, and Mean fluid air speed is 0.5h-1-2h-1.Ether
The catalyst for changing reaction can be Al2O3、Al2O3-SiO2Composite oxides, solid supported acid catalyst and solid supported base catalysis
At least one of agent.It is highly preferred that it is 350-450 DEG C that the condition of the etherification reaction, which includes temperature, Mean fluid air speed is
0.5h-1-1.0h-1, the catalyst of etherification reaction is Al2O3-SiO2Composite oxides, with Al2O3-SiO2Composite oxides it is total
On the basis of amount, SiO2Content be 35-70 weight %.
It is also preferable that remaining alcohol as recycle alcohol is incorporated to step after carrying out etherification reaction in step (5) of the present invention
(2) methanol obtained in, the carbolic oil fraction obtained with step (4) carry out etherification reaction.
In step (6) of the present invention, the condition of the hydrofinishing may include: that reaction temperature can be 350-400 DEG C, pressure
Power can be 8-20MPa, and hydrogen to oil volume ratio can be 800-2000:1, and Mean fluid air speed can be 0.5h-1-3h-1。
According to the present invention, the hydrofining reaction preferably carries out in the presence of a catalyst, and the catalyst is not specific
Limit, can be the conventional selection of this field, the catalyst is conventional Hydrobon catalyst, mainly with group VIB and
Group VIII metal is active component, and vib metals are generally Mo and/or W, group VIII metal Co and/or Ni, with siliceous
Aluminium oxide or aluminium oxide are carrier
It is highly preferred that it is 360-380 DEG C that the condition of the hydrofining reaction, which includes: reaction temperature, pressure 10-
20MPa, hydrogen to oil volume ratio 1000-2000:1, Mean fluid air speed are 0.8h-1-2h-1。
Preferably, in the fractional distillation process of step (6) of the present invention, the boiling range temperature range of gasoline component is 65-195 DEG C, bavin
The boiling range temperature of oil ingredient can be 220-365 DEG C.
The method of coal clean fuel provided by the invention obtains antiknock component, by by this high-octane rating group
Divide and be added in gasoline component, obtains gasoline that meet national standards to realize using coal as raw material, it is preferable that this hair
The blending weight ratio for the gasoline component that the antiknock component and step (6) fractionation that bright step (5) obtains obtain can be 1:
0.3-7。
It is described the prefered embodiments of the present invention in detail above in conjunction with attached drawing, still, the present invention is not limited to above-mentioned realities
The detail in mode is applied, within the scope of the technical concept of the present invention, a variety of letters can be carried out to technical solution of the present invention
Monotropic type, these simple variants all belong to the scope of protection of the present invention.
It is further to note that specific technical features described in the above specific embodiments, in not lance
In the case where shield, can be combined in any appropriate way, in order to avoid unnecessary repetition, the present invention to it is various can
No further explanation will be given for the combination of energy.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should also be regarded as the disclosure of the present invention.
Embodiment 1
Shown in process flow as shown in Figure 1:
(1) it is sent into upright gas retort after crushing feed coal (Shenmu Coal) and carries out pyrolytic reaction, pressure 0.05MPa,
Temperature is 650 DEG C, obtains coal tar (property see the table below 1), semicoke and pyrolysis coal gas.Semicoke is sent into fluidized bed coal gas generator
In, it is 0.13MPa in pressure, temperature is 1000 DEG C, under conditions of gas-solid ratio 5:1 (volume/volume), with vapor and oxygen
(vapor is 4:1 with the volume ratio of oxygen) reacts, and obtains gasification raw gas.Gasification raw gas enters after being pressurized to 3.0MPa
Ingredient in gas is met H in methanol-fueled CLC unstripped gas by sulphur-resistant conversion device2The requirement of/CO, transformed gas enter de-
Total sulfur content in gas is reduced to 0.1ppm hereinafter, filling again through compressor boost to 5.0MPa into methanol-fueled CLC by sulphur device
It sets (fixed bed reactors) and carries out methanol synthesis reaction, the condition of the methanol synthesis reaction includes: that temperature is 260 DEG C, pressure
For 5.0MPa, synthesis gas air speed is 5000h-1；The catalyst of the methanol synthesis reaction is CuO/ZnO/Al2O3；Through rectifying point
From obtaining methanol and methanol purge gas；And mix the pyrolysis coal gas that pyrolytic reaction obtains with methanol purge gas, pass through UF membrane
Method obtains the hydrogen that concentration is greater than 99.8 weight %.
(2) coal tar for obtaining step (1) is after mechanical pretreatment imurity-removal and water, under conditions of 200 DEG C into
Row distillation separation, obtains carbolic oil fraction and heavy end；Wherein, the total amount of phenol is 60 weight % in the carbolic oil fraction；Again will
Phenol and methanol are 1:5 with molar ratio in the carbolic oil fraction, in the case where temperature is 450 DEG C, Mean fluid air speed 1.5h-1, in catalyst
Al2O3In the presence of carry out etherification reaction, as a result obtain high-octane gasoline additive, octane number 111.9.
(3) by obtained heavy end carry out hydrofinishing, reaction temperature be 380 DEG C, pressure 12MPa, hydrogen oil body
For product than being 2000:1, Mean fluid air speed is 1h-1Lower carry out hydrofining reaction, fractionation obtain hydrogasoline, hydrogenated diesel oil and
Hydrogenation tail oil；As shown in Figure 1, by the hydrogenation tail oil recycled again reaction temperature be 400 DEG C, pressure 12MPa, hydrogen oil volume
Than for 1500:1, Mean fluid air speed is 0.8h-1Lower progress hydrocracking reaction obtains cracked oil, and returns to cracked oil and add hydrogen essence
Process processed carries out hydrofinishing together with the heavy end, then is fractionated, and obtains hydrogasoline, hydrogenated diesel oil and adds hydrogen tail
Oil；Then, by hydrogenated diesel oil reaction temperature be 380 DEG C, pressure 12MPa, hydrogen to oil volume ratio 1200:1, Mean fluid is empty
Speed is 0.5h-1Lower carry out hydro-upgrading obtains the modification high 16 value diesel oil of diesel oil-；Then, the production then by etherified reaction obtained
Object antiknock component is mixed with above-mentioned hydrogasoline with the weight ratio of 1:2.8, and blended gasoline end oil product is obtained.
After tested, the ingredient of high-octane gasoline and high 16 value diesel oil, as shown in tables 2 and 3.
1 coal tar oil nature of table
The property of 2 gasoline end oil product of table
Note: No. 93 national standard parameters are GB 17930-2011 " motor petrol " No. 93 motor petrol standard parameters.
3 diesel component property of table
Note: No. 0 national standard parameter is GB 19147-2009 " derv fuel " No. 0 derv fuel standard parameter.
Embodiment 2
Shown in process flow as shown in Figure 2:
(1) it is sent into upright gas retort after crushing feed coal (Shenmu Coal) and carries out pyrolytic reaction, pressure 0.05MPa,
Temperature is 650 DEG C, obtains coal tar (property sees the above table 1), semicoke and pyrolysis coal gas.Semicoke is sent into fluidized bed coal gas generator
In, it is 0.13MPa in pressure, temperature is 1000 DEG C, under conditions of gas-solid ratio 5:1 (volume/volume), with vapor and oxygen
(vapor is 4:1 with the volume ratio of oxygen) reacts, and obtains gasification raw gas.Gasification raw gas enters after being pressurized to 3.0MPa
Ingredient in gas is met H in methanol-fueled CLC unstripped gas by sulphur-resistant conversion device2The requirement of/CO, transformed gas enter de-
Total sulfur content in gas is reduced to 0.1ppm hereinafter, filling again through compressor boost to 6.0MPa into methanol-fueled CLC by sulphur device
It sets (fixed bed reactors) and carries out methanol synthesis reaction, the condition of the methanol synthesis reaction includes: that temperature is 270 DEG C, pressure
For 6.0MPa, synthesis gas air speed is 6000h-1；The catalyst of the methanol synthesis reaction is CuO/ZnO/Al2O3；Through rectifying point
From obtaining methanol and methanol purge gas；And mix the pyrolysis coal gas that pyrolytic reaction obtains with methanol purge gas, it is inhaled by transformation
Attached purifying hydrogen of hydrogen method obtains the hydrogen that concentration is greater than 99 weight %.
(2) coal tar for obtaining step (1) is after mechanical pretreatment imurity-removal and water, under conditions of 200 DEG C into
Row distillation separation, obtains carbolic oil fraction (the 60 weight % that the total amount of phenol accounts for carbolic oil fraction quality) and heavy end；It is in temperature
350 DEG C, Mean fluid air speed 1.0h-1Under conditions of, it is the ratio of 1:5 with molar ratio, carbolic oil fraction and step (1) is obtained
Methanol carries out etherification reaction, and the catalyst of etherification reaction is Al2O3.Obtained antiknock component, octane number 109.1.
(3) obtained heavy end is subjected to hydrofinishing, the condition of the hydrofinishing includes: that reaction temperature is 360
DEG C, pressure 20MPa, hydrogen to oil volume ratio 2000:1, Mean fluid air speed be 2h-1.Refined products are fractionated, and obtain adding hydrogen vapour
Oil, hydrogenated diesel oil and hydrogenation tail oil.
(4) as shown in Fig. 2, by tail oil component reaction temperature is 380 DEG C, pressure 20MPa, hydrogen to oil volume ratio are
1200:1, Mean fluid air speed are 1.2h-1Lower progress hydrocracking reaction obtains cracked oil, cracking oil product return step (3) with
It is fractionated again after refined products mixing, obtains hydrogasoline, hydrogenated diesel oil and hydrogenation tail oil.(5) step (2) are etherified to obtained height
Octane components are mixed with the gasoline fraction that step (4) fractionation obtains with the weight ratio of 1:2.2, obtained gasoline end oil product
Property it is as shown in table 4.
(6) diesel oil distillate obtained step (4) carries out hydro-upgrading, and reaction temperature is 400 DEG C, pressure 20MPa, hydrogen
Oil volume ratio is 1200:1, and Mean fluid air speed is 1.5h-1；The property of diesel component is as shown in table 5 after hydro-upgrading.
The property of 4 gasoline end oil product of table
Note: No. 93 national standard parameters are GB 17930-2011 " motor petrol " No. 93 motor petrol standard parameters.
The property of diesel component after 5 hydro-upgrading of table
Note: No. 0 national standard parameter is GB 19147-2009 " derv fuel " No. 0 derv fuel standard parameter.
Embodiment 3
Shown in process flow as shown in Figure 3:
(1) it is sent into upright gas retort after crushing feed coal (Shenmu Coal) and carries out pyrolytic reaction, pressure 0.05MPa,
Temperature is 650 DEG C, obtains coal tar (property sees the above table 1), semicoke and pyrolysis coal gas.Semicoke is sent into gasification furnace, in pressure
For 3MPa, temperature is 1200 DEG C, under conditions of gas-solid ratio 6:1 (volume/volume), with vapor and oxygen (vapor and oxygen
Volume ratio be 5:1) reaction, obtain gasification raw gas.The raw gas that gasifies enters sulphur-resistant conversion device after being pressurized to 3.0MPa,
Ingredient in gas is met to the requirement of H2/CO in methanol-fueled CLC unstripped gas, transformed gas enters desulfurizer, by gas
Middle total sulfur content is reduced to 0.1ppm hereinafter, again through compressor boost to 5.0MPa, into methanol synthesizer (fixed bed reaction
Device) methanol synthesis reaction is carried out, the condition of the methanol synthesis reaction includes: that temperature is 260 DEG C, pressure 5.0MPa, synthesis
Gas air speed is 5000h-1；The catalyst of the methanol synthesis reaction is CuO/ZnO/Al2O3；Through the isolated methanol of rectifying and
Methanol purge gas；And mix the pyrolysis coal gas that pyrolytic reaction obtains with methanol purge gas, by Pressure Swing Adsorption hydrogen method,
Obtain the hydrogen that concentration is greater than 99 weight %.
(2) coal tar for obtaining step (1) is after mechanical pretreatment imurity-removal and water, under conditions of 200 DEG C into
Row distillation separation, obtains carbolic oil fraction (the 60 weight % that the total amount of phenol accounts for carbolic oil fraction quality) and heavy end；It is in temperature
400 DEG C, be the ratio of 1:3 with molar ratio, by phenol in the presence of catalyst Al2O3 under conditions of Mean fluid air speed 0.5h-1
The methanol that oil distillate and step (1) obtain carries out etherification reaction, obtained antiknock component, octane number 120.5.
(3) obtained heavy end is subjected to hydrofinishing, the condition of the hydrofinishing includes: that reaction temperature is 380
DEG C, pressure 10MPa, hydrogen to oil volume ratio 2000:1, Mean fluid air speed be 0.8h-1；Refined products, which are fractionated, to be obtained adding hydrogen
Gasoline, hydrogenated diesel oil and hydrogenation tail oil.
(4) as shown in figure 3, by tail oil group lease making circulate in reaction temperature be 400 DEG C, pressure 10MPa, hydrogen to oil volume ratio
For 2000:1, Mean fluid air speed is to carry out hydrocracking reaction under 0.6h-1 to obtain cracked oil, and return the part cracked oil
Unifining process is returned, hydrofinishing is carried out together with the heavy end, the part cracked oil mixes again with refined products
It is fractionated, obtains hydrogasoline, hydrogenated diesel oil and hydrogenation tail oil.
(5) by the antiknock component that step (2) etherificate obtains and the gasoline fraction that step (4) fractionation obtains with 1:6.8
Weight ratio mixed, the property of obtained gasoline end oil product is as shown in table 6.
(6) diesel oil distillate obtained step (4) carries out hydro-upgrading, and reaction temperature is 380 DEG C, pressure 10MPa, hydrogen
Oil volume ratio is 2000:1, and Mean fluid air speed is 1h-1；The property of diesel component is as shown in table 7 after hydro-upgrading.
The property of 6 gasoline end oil product of table
Note: No. 93 national standard parameters are GB 17930-2011 " motor petrol " No. 93 motor petrol standard parameters.
The property of diesel component after 7 hydro-upgrading of table
Note: No. 0 national standard parameter is GB 19147-2009 " derv fuel " No. 0 derv fuel standard parameter.
Embodiment 4
Shown in process flow as shown in Figure 3:
(1) it is sent into upright gas retort after crushing feed coal (Hulun Buir coal) and carries out pyrolytic reaction, pressure is
0.03MPa, temperature are 550 DEG C, obtain coal tar (property see the table below 8), semicoke and pyrolysis coal gas.Semicoke is sent into gasification furnace
In, it is 2.8MPa in pressure, temperature obtains gasification raw gas under the conditions of being 1200 DEG C.Raw gas gasify after being pressurized to 3.0MPa
Into sulphur-resistant conversion device, the ingredient in gas is met into H in methanol-fueled CLC unstripped gas2The requirement of/CO, transformed gas into
Enter desulfurizer, total sulfur content in gas is reduced to 0.1ppm hereinafter, closing again through compressor boost to 5.0MPa into methanol
Methanol synthesis reaction is carried out at device (fixed bed reactors), the condition of the methanol synthesis reaction includes: that temperature is 260 DEG C,
Pressure is 5.0MPa, and synthesis gas air speed is 4000h-1；The catalyst of the methanol synthesis reaction is CuO/ZnO/Al2O3；Through essence
Evaporate isolated methanol and methanol purge gas；And mix the pyrolysis coal gas that pyrolytic reaction obtains with methanol purge gas, pass through change
Pressure absorption purifying hydrogen of hydrogen method, obtains the hydrogen that concentration is greater than 99 weight %.
(2) coal tar for obtaining step (1) is after mechanical pretreatment imurity-removal and water, under conditions of 180 DEG C into
Row distillation separation, obtains carbolic oil fraction (the 64 weight % that the total amount of phenol accounts for carbolic oil fraction quality) and heavy end；It is in temperature
400 DEG C, Mean fluid air speed 0.5h-1Under conditions of, it is the ratio of 1:5 with molar ratio, in catalyst Al2O3-SiO2Combined oxidation
(with Al in the presence of object2O3-SiO2On the basis of the total amount of composite oxides, SiO2Content be 60 weight %) by carbolic oil fraction with
The methanol that step (1) obtains carries out etherification reaction, obtained antiknock component, octane number 120.5.
(3) obtained heavy end is subjected to hydrofinishing, the condition of the hydrofinishing includes: that reaction temperature is 380
DEG C, pressure 12MPa, hydrogen to oil volume ratio 1000:1, Mean fluid air speed be 2h-1；Refined products, which are fractionated, to be obtained adding hydrogen vapour
Oil, hydrogenated diesel oil and hydrogenation tail oil.
(4) as shown in figure 3, by tail oil group lease making circulate in reaction temperature be 400 DEG C, pressure 12MPa, hydrogen to oil volume ratio
For 2000:1, Mean fluid air speed is 2h-1Lower progress hydrocracking reaction obtains cracked oil, and returns to the part cracked oil and add
Hydrogen subtractive process, carries out hydrofinishing together with the heavy end, and the part cracked oil is mixed again with refined products through dividing
It evaporates, obtains hydrogasoline, hydrogenated diesel oil and hydrogenation tail oil.
(5) by the antiknock component that step (2) etherificate obtains and the gasoline fraction that step (4) fractionation obtains with 1:6.0
Weight ratio mixed, the property of obtained gasoline end oil product is as shown in table 6.
(6) diesel oil distillate for obtaining step (4) carries out hydro-upgrading, and reaction temperature is 400 DEG C, pressure 12MPa, hydrogen
Oil volume ratio is 1000:1, and Mean fluid air speed is 1h-1；The property of diesel component is as shown in table 7 after hydro-upgrading.
8 coal tar oil nature of table
The property of 9 gasoline end oil product of table
Note: No. 93 national standard parameters are GB 17930-2011 " motor petrol " No. 93 motor petrol standard parameters.
The property of diesel component after 10 hydro-upgrading of table
Note: No. 0 national standard parameter is GB 19147-2009 " derv fuel " No. 0 derv fuel standard parameter.
Embodiment 5
Shown in process flow as shown in Figure 3:
(1) it is sent into upright gas retort after crushing feed coal (Hulun Buir coal) and carries out pyrolytic reaction, pressure is
0.03MPa, temperature are 550 DEG C, obtain coal tar (property sees the above table 8), semicoke and pyrolysis coal gas.Semicoke is sent into gasification furnace
In, it is 3MPa in pressure, temperature obtains gasification raw gas under the conditions of being 1200 DEG C.The raw gas that gasifies is laggard through being pressurized to 3.0MPa
Enter sulphur-resistant conversion device, the ingredient in gas is met into H in methanol-fueled CLC unstripped gas2The requirement of/CO, transformed gas enter
Total sulfur content in gas is reduced to 0.1ppm hereinafter, again through compressor boost to 5.0MPa, into methanol-fueled CLC by desulfurizer
Device (fixed bed reactors) carries out methanol synthesis reaction, and the condition of the methanol synthesis reaction includes: that temperature is 260 DEG C, pressure
Power is 5.0MPa, and synthesis gas air speed is 4000h-1；The catalyst of the methanol synthesis reaction is CuO/ZnO/Al2O3；Through rectifying
Isolated methanol and methanol purge gas；And mix the pyrolysis coal gas that pyrolytic reaction obtains with methanol purge gas, pass through transformation
Purifying hydrogen of hydrogen method is adsorbed, the hydrogen that concentration is greater than 99 weight % is obtained.
(2) coal tar for obtaining step (1) is after mechanical pretreatment imurity-removal and water, under conditions of 180 DEG C into
Row distillation separation, obtains carbolic oil fraction (the 64 weight % that the total amount of phenol accounts for carbolic oil fraction quality) and heavy end；It is in temperature
400 DEG C, Mean fluid air speed 0.5h-1Under conditions of, it is the ratio of 1:5 with molar ratio, in catalyst Al2O3-SiO2Combined oxidation
(with Al in the presence of object2O3-SiO2On the basis of the total amount of composite oxides, SiO2Content be 55 weight %) by carbolic oil fraction with
The methanol that step (1) obtains carries out etherification reaction, obtained antiknock component, octane number 120.5.
(3) obtained heavy end is subjected to hydrofinishing, the condition of the hydrofinishing includes: that reaction temperature is 380
DEG C, pressure 8MPa, hydrogen to oil volume ratio 2000:1, Mean fluid air speed are 0.8h-1；Refined products, which are fractionated, to be obtained adding hydrogen vapour
Oil, hydrogenated diesel oil and hydrogenation tail oil.
(4) as shown in figure 3, by tail oil group lease making circulate in reaction temperature be 400 DEG C, pressure 8MPa, hydrogen to oil volume ratio
For 2000:1, Mean fluid air speed is 0.8h-1Lower progress hydrocracking reaction obtains cracked oil, and returns to the part cracked oil
Unifining process carries out hydrofinishing together with the heavy end, and the part cracked oil is mixed with refined products to pass through again
Fractionation obtains hydrogasoline, hydrogenated diesel oil and hydrogenation tail oil.
(5) by the antiknock component that step (2) etherificate obtains and the gasoline fraction that step (4) fractionation obtains with 1:4.8
Weight ratio mixed, the property of obtained gasoline end oil product is as shown in table 11.
(6) diesel oil distillate obtained step (4) carries out hydro-upgrading, and reaction temperature is 380 DEG C, pressure 10MPa, hydrogen
Oil volume ratio is 2000:1, and Mean fluid air speed is 0.5h-1；The property of diesel component is as shown in table 12 after hydro-upgrading.
The property of 11 gasoline end oil product of table
Note: No. 93 national standard parameters are GB 17930-2011 " motor petrol " No. 93 motor petrol standard parameters.
The property of diesel component after 12 hydro-upgrading of table
Note: No. 0 national standard parameter is GB 19147-2009 " derv fuel " No. 0 derv fuel standard parameter.
The method that can be seen that coal clean fuel provided by the invention from the data in above embodiments and table 1-12 is real
The abundant deep processing to coal resources is showed, has obtained antiknock component, has produced the clean fuel of high-quality, realize simultaneously
System connectivity between each production technology, improving system energy efficiency maximizes utilizing for the energy, has reached coal resources
Efficient and clean utilization.
Claims (9)
1. a kind of method of coal clean fuel, wherein this method comprises:
(1) under the conditions of 450-650 DEG C, feed coal is pyrolyzed, obtains coal tar, semicoke and pyrolysis coal gas；
(2) semicoke that step (1) obtains is obtained into gasification raw gas through gasification, carries out methanol synthesis reaction after transformed, obtains
Methanol and methanol purge gas；
(3) the pyrolysis coal gas that step (1) obtains is mixed with the methanol purge gas that step (2) obtains, and in the case where mentioning hydrogen condition, obtained
To hydrogen；
(4) under conditions of 190-220 DEG C, the coal tar that step (1) obtains is subjected to distillation separation, obtains carbolic oil fraction and again
Matter fraction；
(5) the carbolic oil fraction that step (4) obtains and the methanol that step (2) obtain are subjected to etherification reaction, obtain high-octane rating group
Point；
(6) heavy end for obtaining step (4) carries out hydrofinishing, and refined products are fractionated and obtain gasoline fraction, diesel oil evaporates
Point and tail oil fraction；
(7) antiknock component that step (5) obtains is reconciled with obtained gasoline fraction is fractionated in step (6), is made
High-octane gasoline；
(8) diesel oil distillate is subjected to hydro-upgrading processing, modification diesel oil is made；
(9) by least part hydrogen that step (3) obtains be passed through step (6) hydrofinishing and/or step (8) plus hydrogen change
In qualitative response；
In step (2), the methanol synthesis reaction is carried out on fixed bed reactors, the condition packet of the methanol synthesis reaction
Include: temperature is 220-280 DEG C, pressure 5-10MPa, and synthesis gas air speed is 4000-10000h-1；
In step (5), the condition of the etherification reaction includes that temperature is 350-450 DEG C, and Mean fluid air speed is 0.5h-1-2h-1,
The catalyst of etherification reaction is Al2O3、Al2O3-SiO2Composite oxides, solid supported acid catalyst and solid supported base catalyst
At least one of；
In step (6), the condition of hydrofining reaction includes: that reaction temperature is 350-400 DEG C, pressure 8-20MPa, hydrogen oil body
For product than being 800-2000:1, Mean fluid air speed is 0.5h-1-3h-1。
2. according to the method described in claim 1, wherein, this method further include: added the tail oil fraction that step (6) obtains
Hydrogen cracking, in the refined products that crackate is incorporated to the heavy end that step (4) obtains and/or step (6) obtains；
The condition being hydrocracked includes: that reaction temperature is 360-400 DEG C, pressure 8-20MPa, hydrogen to oil volume ratio 800-
2000:1, Mean fluid air speed are 0.5h-1-3h-1。
3. according to the method described in claim 1, wherein, in step (2), the condition of the gasification includes: that vapor pressure is
0.07-3MPa, gasification temperature are 1000-1200 DEG C.
4. according to the method described in claim 1, wherein, in step (3), the method for mentioning hydrogen is pressure swing adsorption method or film point
From method.
5. according to the method described in claim 1, wherein, in the etherification reaction of step (5), phenol in carbolic oil fraction and methanol
Molar ratio be 1:1-5.
6. according to the method described in claim 1, wherein, in the fractional distillation process of step (6), the boiling range temperature range of gasoline fraction
It is 65-195 DEG C, the boiling range temperature of diesel oil distillate is 220-365 DEG C.
7. according to the method described in claim 1, wherein, the antiknock component that step (5) obtains is obtained with step (6) fractionation
Gasoline fraction weight ratio be 1:0.3-7.
8. according to the method described in claim 1, wherein, in step (8), the condition of the hydro-upgrading includes: reaction temperature
It is 360-400 DEG C, pressure 8-20MPa, hydrogen to oil volume ratio 800-2000:1, Mean fluid air speed are 0.5h-1-3h-1。
9. high-octane gasoline that the method for coal clean fuel according to claim 1 to 8 obtains and changing
Matter diesel oil.
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