CN103992823B - Low-order coal and the method and system that biomass are Material synthesis methane and petrol and diesel oil - Google Patents

Abstract

The invention provides a kind of low-order coal and the method and system that biomass are Material synthesis methane and petrol and diesel oil, described method includes: low-order coal coking is processed, obtains solid product semicoke and gas-phase product, gas-phase product is isolated pyrolysis gas and tar；Solid product semicoke is carried out gasification and obtains char Gasification synthesis gas；Biomass gasified synthesis gas is obtained by after gasification of biomass；Carry out fischer-tropsch reaction after pyrolysis gas, char Gasification synthesis gas and biomass gasified synthesis gas being mixed, then the Oil-gas Separation obtained is obtained artificial oil and unconverted gas；The artificial oil obtained is mixed with tar, distillation obtain temperature less than 180 DEG C, 180 320 DEG C and more than the fraction of 320 DEG C, above-mentioned cut fraction hydrogenation is processed and isolates carbon number lighter hydrocarbons within 4；By carbon number lighter hydrocarbons within 4 and unconverted gas mixing synthesizing methane.The method of the present invention is conducive to the exploitation of extensive development low-order coal, improves the economic benefit of system.

Description

Low-order coal and the method and system that biomass are Material synthesis methane and petrol and diesel oil

Technical field

The present invention relates to a kind of low-order coal and the method and system that biomass are Material synthesis methane and petrol and diesel oil, belong to energy Source fuel and chemical production technical field.

Background technology

The clean coal technology utilizing coal artificial oil fuel certainly will account for master in petroleum replacing produces share Want status.Compare more direct liquid technology, the indirect preparing liquid fuel technology in coal preparing liquid fuel technology path, i.e. Fischer-tropsch synthesis process is carried out for raw material, it is possible to be easier to realize sulfide, nitrogen oxides, heavy hydrocarbon with synthesis gas from coal gasification Class and the qualified discharge of content of beary metal.But, the large-scale application of F-T synthesis technology there is also many restrictions because of Element.Such as, most study still utilizes the quality such as anthracite, bituminous coal preferable i.e. at present, the coal that energy density is higher Carry out gasifying and synthesizing, and the low-order coal (being often referred to brown coal and ub-bituminous coal) that in coal geology storage, ratio is the highest carries out expense The low-order coal the most rarely found report of indirect coal liquefaction route of torr synthesis system synthesis.This contains mainly due in most low-order coal There is higher volatile part, sulfur, wet part and an ash, and the unfavorable factor such as relatively low calorific value about its biggest rule The business application of mould gasification technology.

The scale that systematic study is low-order coal of coal decoupling thermal transition technology utilizes and opens new road.Decoupling thermal transition Technology then can by process intensification or peel off certain in coal gasification course/some specific son reaction (such as, coking, Crack, reform, gasify and burn) and release the coupling of reaction network, and then to by decoupling son reaction carry out restructuring and The most integrated.At present, the pyrolysis RMD fing mode decoupling of coal can form diversified New type coal conversion process, and this mainly includes double bed Gasification, double bed coking/gasification, coal plug technology, two-part gasification, chemical cycle gasification etc..Decoupling thermal transition skill The Successful Practice of art, it is meant that high according to low-order coal fugitive constituent, oil content is high feature, can peel off coal conversion reaction Coking in network, utilizes light hydrocarbons, hydrogen, liquid in Low-temperature carbonization in coal (pyrolysis) technique coal The independence of product (coal tar or coal artificial oil) separates out, and obtains the high-quality semicoke solid of upgrading simultaneously.Ordinary circumstance Under, although coal tar accounts for the mass ratio of coking product and only has 9.0%～15.0%, but its energy density and economy Far above other semicoke and pyrolysis coal gas.Coking of coal product liquid can produce gasoline, bavin through the refined refinement in downstream The transport fuel such as oil and kerosene；And the metallurgical fuel of solid product semicoke the most still high added value and industrial chemicals, also it is Excellent gasified raw material, can build the derived energy chemical platform with synthesis gas as core by char Gasification, produce liquid The downstream product of the high added values such as fluid fuel, electric power, chemicals, thus realize the height of low-order coal thermochemical study process The step coproduction of efficiency, low stain, high product quality and multi-product.

Still further aspect, for directly utilizing the ICL for Indirect Coal Liquefaction skill that coal based synthetic gas is raw material production synthetic liquid fuel Art, if not carrying out reduction of greenhouse gas discharge process, the greenhouse gas discharge capacity of its broad sense fuel recycle process would is that tradition About the twice of crude refining liquid fuel line, thus environment is caused bigger negative effect.If application greenhouse Gas abatement technology, energy and economy cost largely reducing again the competition of it and conventional petroleum preparing liquid fuel route Power.It should be noted that the reason such as significant greenhouse gas emission due to exploitation of coal resources process, even if at coal Use up-to-date carbon dioxide capture and storing technology during preparing liquid fuel, its total greenhouse gas emissions still than Crude oil route is high by more than 25%.The feasibly alternative of the greenhouse gas emissions in reduction F-T synthesis oil production process Case is that this includes biomass and coal gasifies altogether by coal preparing liquid fuel and two PROCESS COUPLING of biomass preparing liquid fuel Individually gasify two schemes.Biomass artificial oil technology can substantially reduce the greenhouse gas of F-T synthesis route Body discharge capacity.Reason is, biomass energy realizes CO from the photosynthesis in growing process₂From So capture, it is relatively low that the net impacts (gather in, transport, store and convert) of weather can be reached substantially by bio-fuel CO₂Discharge, its processed process also close friend gentleer to environment.Such as, result of study is had to show to compare tradition Fossil energy route, the production process of corn alcohol can realize the effect of Life cycle reduction of greenhouse gas discharge more than 50% Really.

Meanwhile, low-order coal coking produces coal tar and the Fischer-Tropsch synthesis oil of F-T synthesis generation need at hydro carbons refined single Unit upgrades to meeting the transport gasoline of fuel standard, diesel oil and by-product Colophonium.Although both raw material oil properties With composition slightly some differences.But both exceed the drawback that technical uncertainty is brought, example at the most refined advantage As, refining altogether and can be greatly saved equipment investment, reduce the complexity of harmonic process, heterogeneity oil product complementation utilizes, Etc..View of the above facts have proved by gyp F-T synthesis oilmill.At present, close for high temperature fischer-tropsch The common refining becoming oil and Low Temperature Fischer Tropsch artificial oil produces diesel oil process, and South Africa Sasol company establishes business in South Africa Ye Xing factory.In lot of documents, especially for the liquid refinery of biomass, natural gas and coal, it is directed to Fischer-Tropsch synthesis oil is make use of to produce motor petrol, diesel oil, aerial kerosene and the process of liquefied petroleum gas.But, the most greatly Department pattern still utilizes experience productivity or produces middle thick product (such as Petroleum and distillate etc.).And for synthesis The detailed process model of oil refining and layout strategy, the document of middle this respect is the fewest over the past thirty years.It is necessary to make The end product of oil product refining scheme reaches the preliminary every basic standard of fuel oil for vehicles, at the octane improving product gasoline Aromatic hydrocarbon content therein is reduced to reach No. four oil product standards EU-4 in Europe while value.

Still further aspect, once can produce a large amount of lighter hydrocarbons by the fischer-tropsch synthesis process of type, mainly from C₁To C₄'s Alkane and alkene, and unreacted CO and H of about about 50%₂.Noticing in above component, lighter hydrocarbons are to close Become the key component of natural gas, CO and H₂It it is then the primary raw material producing synthetic natural gas.Have in view of that, Ke Yigai Become traditional fuel power generation function or circulating reflux method, produce synthetic with the gas of this part high added value natural Gas, thus it is greatly improved energy efficiency and the economy of whole multifunctional energy resource system.By coal liquifaction and natural gas from coal This two intermediate item organic coupling is the most also the efficient utilization of the feature based on domestic energy resource structure, beneficially development of coal Convert with cleaning low-carbon (LC), produce clean energy resource, meet the energy development strategy of " high-carbon energy low carbonization utilization ", to reality The sustainable use of existing coal resources is significant.

Summary of the invention

It is an object of the present invention to provide a kind of low-order coal and the side that biomass are Material synthesis methane and petrol and diesel oil Method；

Another object of the present invention is to provide a kind of low-order coal and biomass be Material synthesis methane and petrol and diesel oil be System.

For reaching above-mentioned purpose, on the one hand, the invention provides a kind of with low-order coal and biomass for Material synthesis methane and The method of petrol and diesel oil, described method includes:

(1) low-order coal coking is processed, obtain solid product semicoke and gas-phase product, wherein gas-phase product is separated Go out pyrolysis gas and tar；

(2) the solid product semicoke of step (1) is carried out gasification and obtain char Gasification synthesis gas；

(3) biomass gasified synthesis gas is obtained by after gasification of biomass；

(4) by the pyrolysis gas of step (1), the char Gasification synthesis gas of step (2) and the biomass of step (3) Carry out fischer-tropsch reaction after gasification synthesis gas mixing, then the Oil-gas Separation obtained is respectively obtained artificial oil and unconverted gas Body；

(5) tar that artificial oil step (4) obtained obtains with step (1) mixes, and enters hydro carbons recovery Column distillation respectively obtain temperature less than 180 DEG C, 180-320 DEG C and more than the fraction of 320 DEG C, above-mentioned fraction is entered respectively Row hydrotreating；

(6) by after the unconverted gas mixing of the carbon number of step (5) lighter hydrocarbons within 4 and step (4) For synthesizing methane.

According to method of the present invention, preferred steps of the present invention (1) is will to carry out coking after low-order coal pretreatment again Process；

According to method of the present invention, the most further preferred described pretreatment is sized to particle diameter for low-order coal being ground For the granule of 80-400mm, then it is dried to humidity less than 8%.

According to method of the present invention, it is to enter in the presence of air and middle pressure steam that the coking of step (1) processes Row；Wherein preferably medium pressure steam is the pressure steam at 25atm；

According to method of the present invention, it is to carry out in the presence of ferrous oxide that the most preferred described coking processes；

The most described ferrous oxide is FeO_x, FeO and Fe₂O₃In the mixing of one or more；

According to method of the present invention, wherein it is also preferred that the reaction temperature that coking processes is 400 DEG C～600 DEG C, Pressure 25atm.

According to method of the present invention, after preferred steps of the present invention (1) obtains solid product semicoke and gas-phase product, Wherein by gas-phase product through solid impurity separating treatment, then isolate pyrolysis gas and tar.Gas-phase product is through solid After magazins' layout processes, the ash carried secretly in gas-phase product and semicoke granule can be removed.

According to method of the present invention, preferred steps of the present invention (2) is to be existed by the solid product semicoke of step (1) Carry out gasification in the presence of oxygen gas and water and high steam and obtain char Gasification synthesis gas.

The wherein the most described steam that high steam is pressure 40atm.

The wherein present invention further preferred oxygen carbon mass ratio 0.5-0.8, water carbon mass ratio is 0.8-1.2.

According to method of the present invention, the gasification of step of the present invention (2) is this area routine operation, such as this The bright gasification reaction conditions that preferably employs be temperature be 1400 DEG C-1700 DEG C, pressure about 40atm.

According to method of the present invention, wherein biomass and low-order coal weight described in preferred step of the present invention (3) Ratio is 0.50～1.5.

According to method of the present invention, the further preferred step of the present invention (3) is that biomass first carry out pretreatment, Carry out gasification again and obtain biomass gasified synthesis gas；

Wherein said pretreatment can be the pretreatment operation that this area is conventional, and the preferred described pretreatment of the present invention is for by raw Material grinds and is sized to the granule that particle diameter is 200-400mm, then is dried to humidity less than 8%；

According to method of the present invention, the gasification described in step of the present invention (3) is the biogas that this area is conventional Changing operation, preferred for this invention is temperature 1200 DEG C-1500 DEG C, pressure about 30atm；

According to method of the present invention, described fischer-tropsch reaction is referred to art methods, the preferred institute of the present invention The condition stating fischer-tropsch reaction is: temperature 310-370 DEG C, and catalyst is Co or Ru series catalysts；

The most further preferred described catalyst is Ru, TiO₂、Co、Zr、SiO₂With the one in MgO or two Plant above combination；

Wherein it is more preferably Ru/TiO₂、Co/Zr/SiO₂Or Co/MgO/SiO₂；It is understood that here/table Show the mixture of material before and after it；

According to method of the present invention, preferred steps of the present invention (4) is by the pyrolysis gas of step (1), step (2) Char Gasification synthesis gas and step (3) biomass gasified synthesis gas mixing after gaseous mixture first passed through CO conversion Reaction carries out fischer-tropsch reaction again；

According to method of the present invention, wherein preferably through the H of gaseous mixture after CO transformationreation₂The mol ratio of/CO For 1.3-2.4；Wherein it is more preferably 1.5.

Wherein said CO transformationreation can be the high temperature CO transformationreation that prior art is conventional, the such as present invention Preferably reaction condition is temperature 500-700 DEG C, and pressure is 25atm, and catalyst is Fe or Cu series catalysts；

The most further preferably by gaseous mixture after CO transformationreation, by gaseous mixture through NHD (NHD) Absorb, then carry out fischer-tropsch reaction；

After can also absorbing preferably through NHD according to the present invention, the CO in gaseous mixture₂And H₂S content removes respectively To 500ppm and below 25ppm.

According to method of the present invention, described in preferred steps of the present invention (5), carry out hydroprocessing operations bag respectively Include and boiling temperature is carried out hydrofinishing less than the fraction of 180 DEG C (Petroleums) and 180-320 DEG C (distillate)；

Wherein after the preferred hydrofinishing of the present invention, cut by fraction collect respectively carbon number lighter hydrocarbons within 4, Carbon number be the component of 5-6, carbon number be the component of 7-12, carbon number be the component of 13-20；

Wherein said hydrofinishing can be the hydrofinishing that this area is conventional, and present invention institute is the most anti- Answer condition be catalyst be SiO₂-Al₂O₃Type catalyst, pressure 35-65atm, temperature 350-500 DEG C, hydrogen oil mole Compare 5-10:1；

According to method of the present invention, the carbon number wherein separated lighter hydrocarbons within 4 can and step (4) for synthesizing methane after unconverted gas mixing；

Wherein carbon number is that the component of 5-6 may be isomerized as auxiliary agent to improve the octane number of gasoline；

Described isomerization can be the isomerization that this area is conventional, the wherein reaction bar of the further preferred isomerization of the present invention Part be catalyst be B₂O₃-Al₂O₃Type catalyst, pressure 30-40atm, temperature 320-450 DEG C, hydrogen/oil mol ratio 5-10:1；

Wherein carbon number is that the component of 7-12 can carry out hydrogenation type catalytic reforming reaction as auxiliary agent to improve gasoline Octane number；

Wherein said hydrogenation type catalytic reforming reaction can be the hydrogenation type catalytic reforming operation that this area is conventional, the present invention Further preferred hydrogenation type catalytic reforming reaction condition be catalyst be Pt/L-type zeolite, pressure 30-40atm, temperature Spend 350-500 DEG C, hydrogen/oil mol ratio 5-10:1；

Wherein carbon number is that the component of 13-20 is as diesel oil head product；

According to method of the present invention, the present invention can with the hydrotreating described in preferred steps (5) also include by The boiling point fraction more than 320 DEG C is hydrocracked；Isocrackate is divided into four strands: 1) carbon number 4 with In lighter hydrocarbons gas, 2) carbon number be the component of 5-6,3) carbon number is the component and 4 of 13-20) remaining Component；

Wherein said being hydrocracked can be the conventional hydrocracking operation in this area, and currently preferred hydrogenation splits Changing reaction condition is with magnesium silicate molecular sieve as catalyst, pressure 35-65atm, temperature 400-600 DEG C, hydrogen oil mole Compare 8-15:1；

According to method of the present invention, wherein carbon number lighter hydrocarbons gas within 4 can with step (4) not For synthesizing methane after reformed gas mixing；

Carbon number is that the component of 5-6 may be isomerized as auxiliary agent to improve the octane number of gasoline；

Wherein said isomerisation conditions can consistent with above-mentioned isomerisation conditions (catalyst be B₂O₃-Al₂O₃Type catalyst, Pressure 30-40atm, temperature 320-450 DEG C)；

Wherein said carbon number is that the component of 5-6 can process generation with the temperature cut fraction hydrogenation less than 180 DEG C Carbon number be 5-6 component mixing after carry out isomerization in the lump；

Wherein carbon number is that the component of 13-20 can be directly as diesel oil head product；

Wherein remaining component can carry out non-hydrogenation catalyst reformation as auxiliary agent to improve the octane number of gasoline；

Wherein said non-hydrogenation catalyst the condition of reorganization is ZSM-5 catalyst, pressure 25-45atm, temperature 300-500 DEG C)；

In remaining component the most above-mentioned, the component of only 60%～80% participates in this reforming reaction and produces reformation body, remaining 20%-40% component directly mixes as gasoline head product with reformation afterproduct；

According to method of the present invention, being separated into this area routine operation altogether described in step (5), the present invention is excellent Selecting in step (5) is to be processed by the hydrogenation of tar of step (1), then the artificial oil obtained with step (4) is carried out altogether Separate；

According to method of the present invention, after the preferred hydrotreating of the present invention, the H/C mol ratio of tar is 0.7-1.2； Wherein it is more preferably 0.85；

According to method of the present invention, wherein said hydrotreating is this area routine operation, and such as the present invention is excellent The reaction condition of hydrotreating of choosing be catalyst be FeS-Fe₂O₃Type catalyst, pressure 30-40atm, temperature 250-350℃。

According to method of the present invention, the carbon number of preferred steps of the present invention (5) lighter hydrocarbons within 4 and step Suddenly the unconverted gas pressurized of (4) to after 25atm as methanation reaction gas；

According to method of the present invention, the carbon atom of rate-determining steps (5) in the further preferred step of the present invention (6) After counting the unconverted gas mixing of the lighter hydrocarbons within 4 and step (4), gaseous mixture includes that following percent by volume becomes Point: CO:15～25%, H₂: 20～30%, CO₂: 30～40%, CH₄: 7.0～15%, C₂H₆: 5.0～10%, C₂H₄: 3.0～5.0%, C₃H₈: 2.0～4.0%, C₃H₁₀: 1.0～3.0%, C₄H₁₀: 0.5～2%, C₄H₈: 0.5～2%.

According to method of the present invention, by the carbon number of step (5) 4 in preferred steps of the present invention (6) Within lighter hydrocarbons and step (4) unconverted gas mixing after first carry out pre-methanation resynthesis methane；

Described pre-methane turns to this area routine operation, and reaction condition the most preferred for this invention is that catalyst is SiO₂Type catalyst, pressure 20-30atm, temperature 400-500 DEG C.Wherein further preferably by the carbon of step (5) CO is first carried out after the unconverted gas mixing of atomic number lighter hydrocarbons within 4 and step (4)₂Membrance separation, more pre-first Alkanisation, then synthesizing methane；

Wherein said membrance separation is this area routine operation, and such as the present invention preferably carries out CO₂After membrance separation, gas CO in body₂Percent by volume is less than 2.0%.

On the other hand, present invention also offers a kind of low-order coal and biomass be Material synthesis methane and petrol and diesel oil be System, described system includes: low-order coal cracking units 2, coal tar recovering equipment 4, char Gasification unit 6, biology Matter gasification unit 8, synthesis gas blender 9, Fischer-Tropsch synthesis device 12, oil gas diverter 13, oil product refine list altogether Unit 14, unstripped gas blender 15, methanator 18；Wherein low-order coal enters low-order coal cracking units 2, To gas-phase product and solid product semicoke, wherein gas-phase product is transported to coal tar recovering equipment 4, isolate tar and Pyrolysis gas, its coal-tar middle oil oil product that is transported to refines unit 14 altogether；The solid obtained in low-order coal cracking units 2 Product semicoke is transported to char Gasification unit 6, obtains char Gasification synthesis gas；Biomass are at gasification of biomass unit Obtaining biomass gasified synthesis gas in 8, wherein pyrolysis gas, char Gasification synthesis gas and biomass gasified synthesis gas are defeated Delivering to synthesis gas blender 9 mix, gaseous mixture is transported to Fischer-Tropsch synthesis device 12 to carry out fischer-tropsch reaction and obtains To oil gas, oil gas is transported to oil gas diverter 13, isolates artificial oil and unconverted gas, and wherein artificial oil is defeated Deliver to oil product refine altogether unit 14 and tar carry out being divided into from, the carbon number of isolated lighter hydrocarbons within 4 and The isolated unconverted gas of oil gas diverter 13 is transported in unstripped gas blender 15 respectively, is then sent to Methanator 18 synthesizing methane.

According to system of the present invention, described system includes: low-order coal pretreatment unit 1, low-order coal cracking units 2, solid impurity separator 3, coal tar recovering equipment 4, air-separating plant 5, char Gasification unit 6, biology Matter pretreatment unit 7, gasification of biomass unit 8, synthesis gas blender 9, synthesis gas CO shift-converter 10, Purified synthesis gas unit 11, Fischer-Tropsch synthesis device 12, oil gas diverter 13, oil product refine unit 14, raw material altogether Gas blender 15, CO₂Membrane separation plant 16, pre-methanator 17, methanator 18；Wherein low order Coal pretreatment unit 1 is connected with low-order coal cracking units 2, and the gas-phase product obtained in low-order coal cracking units 2 is successively By solid impurity separator 3 and coal tar recovering equipment 4, coal tar recovering equipment 4 and oil product refine unit 14 altogether Connecting, the solid product semicoke obtained in low-order coal cracking units 2 is transported to char Gasification unit 6；Biomass warp Cross biomass pretreatment unit 7 and be transported to gasification of biomass unit 8；Air is isolated through air-separating plant 5 Oxygen be passed through char Gasification unit 6, char Gasification unit 6, gasification of biomass unit 8 and coal tar recovering equipment 4 are connected with synthesis gas blender 9 respectively so that from the pyrolysis gas of coal tar recovering equipment 4, from char Gasification The char Gasification synthesis gas of unit 6 and the biomass gasified synthesis gas from gasification of biomass unit 8 mix at synthesis gas In device 9 mix, synthesis gas blender 9 downstream successively with CO shift-converter 10, purified synthesis gas unit 11, Fischer-Tropsch synthesis device 12 and oil gas diverter 13 connect；Two outlets of oil gas diverter 13 are respectively with oil product altogether Refining unit 14 and unstripped gas blender 15 connect；Oil product is refined an outlet of unit 14 altogether and is mixed with unstripped gas Device 15 connects so that oil gas diverter 13 unconverted gas out and oil product are refined the carbon number of unit 14 altogether and existed Lighter hydrocarbons within 4 sequentially pass through CO after unstripped gas blender 15 mixes again₂Membrane separation plant 16, pre-methanation are anti- Device 17 is answered to enter into methanator 18；

According to system of the present invention, wherein said low-order coal cracking units 2 can use prior art routine to set Standby, the present invention is preferably fixed bed reactors；

According to system of the present invention, wherein said char Gasification unit 6 can use prior art conventional equipment, The present invention preferably starches fluidized gas producer；

According to system of the present invention, wherein said gasification of biomass unit 8 can use prior art routine to set Standby, the present invention is preferably as fluidized-bed gasification furnace；

According to system of the present invention, it can be that prior art is conventional that wherein said oil product refines unit 14 altogether Oil product refining plant altogether, the oil product that wherein present invention further preferably uses is refined unit altogether and is included, with coal tar recovering The coal tar hydrogenating processing means that equipment 4 connects, coal tar hydrogenating process after with oil gas diverter 13 synthesis out Oil enters hydro carbons recovery tower and separates；

According to system of the present invention, wherein the outlet of the present invention further preferred hydro carbons recovery tower connects stone brain respectively Oil hydrotreater, distillate hydrogenation processing means and wax hydrofining cracking unit so that the Petroleum separated, Distillate and paraffin oil are admitted to naphtha hydrotreater, distillate hydrogenation processing means and wax hydrofining respectively and split Gasifying device；

According to system of the present invention, wherein the oil product of the present invention is refined unit 14 altogether and is farther included Pt-zeolite Reformer, the carbon number for separating the Petroleum after hydrotreating is more than the component of 6 to be carried out at dehydrogenation Reason；

According to system of the present invention, wherein the oil product of the present invention is refined unit 14 altogether and is farther included isomery makeup Putting, the component that carbon number is 5-6 in the paraffin oil that will separate carries out isomerization；

According to system of the present invention, wherein the oil product of the present invention is refined unit 14 altogether and is farther included non-hydrogenation type ZSM-5 catalytic reforming unit, for paraffin oil is separated except carbon number be 2-4,5-6 and 13-20 Other components in addition carry out isomerization.

In sum, the invention provides a kind of low-order coal and biomass be Material synthesis methane and the method for petrol and diesel oil and System.The method and system of the present invention have the advantage that

1, the low-order coal of the present invention and the multifunctional energy resource system of biomass alliance, first carried by cascade utilization low-order coal For the tar of high added value therein, then Appropriate application solid therein semicoke product, it is not only advantageous to extensive development The exploitation of low-order coal and conversion, substantially increase the economic benefit of system simultaneously.

2, the low-order coal of the present invention and the multifunctional energy resource system of biomass alliance, by adding parallel biogas Gasifying device, by coal preparing liquid fuel and two PROCESS COUPLING of biomass preparing liquid fuel, reduces coal liquifaction flexibly and easily Life cycle greenhouse gas emissions in production process.

3, the low-order coal of the present invention and the multifunctional energy resource system of biomass alliance, by adding parallel biogas Gasifying device, by coal preparing liquid fuel and two PROCESS COUPLING of biomass preparing liquid fuel, reduces coal liquifaction flexibly and easily Life cycle greenhouse gas emissions in production process.

4, the low-order coal of the present invention and the multifunctional energy resource system of biomass alliance, by changing traditional fuel power generation function Or circulating reflux method, once will can produce a large amount of lighter hydrocarbons (C by the fischer-tropsch synthesis process of type₁～C₄) peace treaty is the most anti- The synthesis gas answered is as the raw material of productive manpower synthetic natural gas, thus is greatly improved whole multifunctional energy resource system energy Efficiency and economy.

5, the method that the refining of the present invention meets the vapour of automobile-use standard, diesel oil, by common refining coal tar and height Temperature Fischer-Tropsch synthesis oil, can be greatly saved equipment investment, reduces the complexity of harmonic process, makes full use of two kinds of dissimilarity Matter oil product complementation utilizes, and the product making final oil product refine scheme reaches the preliminary every basic standard of fuel oil for vehicles, Aromatic hydrocarbon content therein is reduced to reach No. four oil product standards in Europe while improving the octane number of product gasoline EU-4。

Accompanying drawing explanation

Low-order coal and biomass that Fig. 1 provides for the present invention are the multi-functional of raw material production vapour, diesel oil and synthetic natural gas Energy resource system schematic diagram.

Detailed description of the invention

Implementation process and the beneficial effect of generation of the present invention is described in detail, it is intended to help to read below by way of specific embodiment Reader is more fully understood that essence and the feature of the present invention, not as can the restriction of practical range to this case.

Embodiment 1

Fig. 1 is the low-order coal that invention provides and the multi-functional energy that biomass are raw material production vapour, diesel oil and synthetic natural gas Origin system schematic diagram.Wherein, S1 to S37 represents each stock trunk gas/liquid logistics of system, and V1 to V9 represents system Each stock steam.Wherein S1 is low-order coal, S2 and S11 is air, and S3 is biomass, S6 and S8 is oxygen, S4 and S10 is the water of removing, and wherein S7 is gasification water, and S12 is the gas-phase product that low-order coal coking processes, S14 For solid product semicoke, S15 is char Gasification synthesis gas, and S20 is pyrolysis gas, and S21 is pyrolysis gas, char Gasification Synthesis gas and the gaseous mixture of biomass gasified synthesis gas, S22 is biomass gasified synthesis gas, and S24 is tar, S26 For hydrogen, S27 is artificial oil, and S29 is the oil gas that fischer-tropsch reaction obtains, and S30 is unconverted gas, and S31 is light Hydrocarbon, S32, S33 are diesel oil and hydrocarbon product, and S34 is lighter hydrocarbons and the methanation unstripped gas of unconverted gas mixing, S5, S9, S19, S25, S28, S35, S36, S37 are the material through respective handling, S13, S16, S17, S18, S23 are the waste discharged.

Capital equipment has low-order coal pretreatment unit 1, low-order coal cracking units 2, solid impurity separator 3, coal tar Recovery of oil equipment 4, air-separating plant 5, char Gasification unit 6, biomass pretreatment unit 7, gasification of biomass Unit 8, synthesis gas blender 9, synthesis gas CO shift-converter 10, purified synthesis gas unit 11, F-T synthesis Reactor 12, oil gas diverter 13, oil product refine unit 14, unstripped gas blender 15, CO altogether₂Membrane separation plant 16, pre-methanator 17, methanator 18.Wherein low-order coal pretreatment unit 1 and low-order coal coking Unit 2 connects, and it exports one synthesis gas and is total to solid impurity separator 3 coal tar recovering equipment 4 and oil product successively Refining unit 14 connects, and exports another strand of synthesis gas and is connected with char Gasification unit 6；Biomass pretreatment unit 7 Connect with gasification of biomass unit 8；From coal tar recovering equipment 4 and pyrolysis gas, char Gasification unit 6 and synthesis The synthesis gas of gas and gasification of biomass unit 8 jointly synthesis gas blender 9 mix after successively with CO shift-converter 10, purified synthesis gas unit 11 connects, Fischer-Tropsch synthesis device 12 and oil gas diverter 13 connect；Fuel-displaced edema caused by disorder of QI The Fischer-Tropsch synthesis oil of stream device 13 is refined unit 14 altogether and is connected with oil product；The unconverted gas of fuel-displaced gas diverter 13 and oil Product are refined altogether after the lighter hydrocarbons of unit 14 mix in unstripped gas blender 15 and are sequentially passed through CO again₂Membrane separation plant 16, Pre-methanator 17 and methanator 18.

Idiographic flow is: its composition of low-order coal S1(is shown in Table 1) first after low-order coal pretreatment unit 1 is dehydrated and pulverizes (low-order coal is ground and is sized to the granule that particle diameter is 80-400mm, then be dried to humidity less than 8%), and air S4 and middle pressure (25atm) steam V1 enters low-order coal cracking units 2 together, and in warp, low temperature pyrogenation reacts solid Body product semicoke S14, gas-phase product S12 and ash S13 and a small amount of low-pressure steam V4 of by-product, reaction condition It is that under excess air and middle pressure steam (25atm) atmosphere, reaction temperature is 500 DEG C, pressure 25atm.Gas phase is produced Thing S12, after the refuse S18 such as the ash wherein carried secretly and a small amount of semicoke granule removed by solid impurity separator 3, enters Coal tar recovering equipment 4(oil gas diverter) condensation, quiet put and be layered reclaim tar S24 and pyrolysis gas S20, Produce a small amount of waste water S23 simultaneously.Pyrolysis chemical reaction is shown in that formula 1, major product Mass Distribution are shown in Table 2:

Table 1

Table 2

Solid product semicoke S14 enter together with feedwater S7 char Gasification unit 6 make after water-coal-slurry again with high pressure (40 Atm) (temperature is 1500 in the high-purity oxygen S6 generating gasification reaction of steam V2 and air-separating plant 5 DEG C, pressure about 40atm), after cooling, obtain synthesis gas S15 and by-product middle pressure steam V5.Meanwhile, biological Its composition of matter S3(is shown in Table 1) pulverize and grind that (grinding is sized to particle diameter through biomass pretreatment unit 7 The granule of 200-400mm, then be dried to humidity less than 8%) enter gasification of biomass list 8, carry out gasified reverse equally (temperature 1200 DEG C, pressure about 30atm) synthesis gas S22 and middle steam V6 should be obtained.Conjunction derived above Become gas S15, S22 to mix at synthesis gas blender 9 with pyrolysis gas S20, enter back into CO shift-converter 10(temperature Spend 550 DEG C, pressure 25atm, catalyst is Fe series catalysts) by the H of F-T synthesis unstripped gas active component₂/CO Improve to 1.5(mol ratio).Concrete F-T synthesis unstripped gas composition is as follows:

Table 3

The F-T synthesis unstripped gas S25 going out CO shift-converter 10 is first through synthesis gas clean unit 11, utilizes NHD Solvent is absorbent, removes most H in gas₂S、SO₂With part CO₂(the CO in gaseous mixture₂And H₂S Content is removed to 500ppm and below 25ppm respectively).Clean unstripped gas is with once by without circulation and backflow Mode through Fischer-Tropsch synthesis device 12(occur high temperature fischer-tropsch synthesis, reaction temperature is 320 DEG C, and catalyst is Ru series catalysts), and after reclaiming its side-product middle pressure steam V8, separating high-temp Fischer-Tropsch in oil gas diverter 13 Artificial oil S27 and unconverted gas S30.

Oil-feed product refine mole composition of the high temperature fischer-tropsch artificial oil S27 and tar S20 of unit as shown in table 4 altogether.? Oil product is refined in unit altogether, additionally also has the refinery hydrogen S26 of the high-quality of one outsourcing.First coal tar is carried out Hydrofinishing process (reaction condition be catalyst be FeS-Fe₂O₃Type catalyst, pressure 40atm, temperature 400 DEG C), Tentatively depart from wherein sulfur and improve H/C ratio (mole) to 0.85 of tar molecules.Tar after process closes with Fischer-Tropsch Become oil mixing, and enter a hydro carbons wherein each active component of recovery tower initial gross separation: the temperature fraction less than 180 DEG C The fraction (distillate) of (Petroleum), temperature 180-320 DEG C and the temperature fraction (paraffin oil) more than 320 DEG C, They are admitted to respectively, and petroleum naphtha hydrogenation is refined, fraction oil hydrogenation refining wax hydrofining cracking unit.Petroleum naphtha hydrogenation and Fraction oil hydrogenation refining (reaction condition be catalyst be SiO₂-Al₂O₃Type catalyst, pressure 40atm, temperature 350 DEG C, hydrogen/oil mol ratio 10:1) after carbon number lighter hydrocarbons within 4 can be with the unconverted gas of step (4) For synthesizing methane after mixing；C₅/C₆Component is sent to C₅/C₆By the C of positive structure body in isomerization unit₅/C₆Isomerization (reaction condition be catalyst be B₂O₃-Al₂O₃Type catalyst, pressure 30atm, temperature 400 DEG C, hydrogen oil mole Than 10:1) to improve the octane number of product gasoline；Other carbon number is that the component of 7-12 is then sent to reformer In carry out hydrogenation type catalytic reforming (reaction condition be catalyst be Pt/L type-zeolite, pressure 30atm, temperature 450 DEG C, hydrogen/oil mol ratio 10:1) cycloalkane by wherein 100% and about 60% alkane carries out isomery dehydrogenation and cyclisation respectively Dehydrogenation produces aromatic hydrocarbons and improves the octane number of gasoline S33；Carbon number is that the component of 13-20 is as diesel oil head product S33.The temperature going out hydro carbons recovery tower is more than the fraction (paraffin oil) of 320 DEG C through hydrocracked, treated (reaction bar Part is with magnesium silicate molecular sieve as catalyst, pressure 50atm, temperature 500 DEG C, hydrogen/oil mol ratio 15:1) it is divided into four Stock: 1) C₂/C₃/C₄Lighter hydrocarbons gas S31 pressurization (25atm) after deliver to unstripped gas blender 15 and be previously obtained As methanation reaction gas after the unconverted gas mixing of carbon number lighter hydrocarbons within 4 and step (4)；2) Containing C₅/C₆The C that component streams and above hydrotreating produce₅/C₆C is delivered in logistics mixing₅/C₆Isomerization unit (catalysis Agent is B₂O₃-Al₂O₃Type catalyst, pressure 30atm, temperature 400 DEG C)；3) containing C₁₃～C₂₀Component directly as Diesel oil head product S33；4) remaining component is delivered to non-hydrogenation type ZSM-5 catalytic reforming unit (catalyst is ZSM5 Catalyst, pressure 40atm, temperature 400 DEG C), the alkane renormalization by wherein 60%～80% produces reformation body alkane To increase the octane number of gasoline S33, can effectively control gasoline arene content simultaneously.

Table 4

Go out oil product and refine the lighter hydrocarbons gas S31 of unit 14 and the unconverted gas S30 of fuel-displaced gas diverter 13 altogether former Material gas blender 15 mixes, and the concrete methanation unstripped gas S34 dry gas volumn concentration obtained is as follows: CO: 18.3%、H₂: 25.7%, CO₂: 31.2%, CH₄: 9.8%, C₂H₆: 5.6%, C₂H₄: 3.24%, C₃H₈: 2.50%、C₃H₁₀: 1.90%, C₄H₁₀: 0.95%, C₄H₈: 0.80%.Methanation unstripped gas S34 first passes around One CO₂Membrane separation plant 16, utilizes the membrane material of hollow by CO therein₂Percent by volume is down to less than 2.0% After, enter pre-methanator 17, primary response (2) side reaction (3) (4) occurs, by the C of wherein 98%₂、 C₃And C₄Lighter hydrocarbons be converted into synthesis gas.The unstripped gas entrance methanator going out pre-methanator produces Whole synthetic natural gas (reaction condition be catalyst be SiO₂Type catalyst, pressure 25atm, temperature 500 DEG C), instead The reaction answered is (5) (6), and substantial amounts of middle steam V9 of by-product.Final methanation product gas and petrol and diesel oil Composition is as shown in table 4.

C_nH_m+nH₂O→(n+0.5m)H₂+ nCO, n > 1 (2)

The final methanation product gas product of the present invention meets GB17820-1999 Natural gas standard, belongs to a class sky So gas.Its dry gas percent by volume is: CH₄: 95.3%, CO₂: 1.5%, H₂: 1.25% and C_nH_m: 1.95% (n > 1), low heat valve 32.0MJ/m³, high calorific power 35.8MJ/m³。

For the advantage of present system is more preferably described, a point product system for native system with reference is carried out Performance comparision, respectively It is coal liquifaction system, natural gas from coal system, biomass oil plant and biomass preparing natural gas system, it is shown in Table 5 Shown in.Definition (7) (8) according to relative energy saving ratio, in the accumulative greenhouse of the Life cycle that design requires On the premise of gas discharge reaches conventional petroleum route, the fractional energy savings of native system still can reach 19.8%.

Table 5

$\begin{array}{c}\mathrm{PES}=\frac{E_{\mathrm{ref}}-E_{\mathrm{mfe}}}{E_{\mathrm{ref}}}=\frac{\underset{i=1}{\overset{p}{\mathrm{\Σ}}}(E_{P_i}/\stackrel{\‾}{{\mathrm{\η}}_i})-\underset{j=1}{\overset{f}{\mathrm{\Σ}}}{E}_{F_j}}{\underset{i=1}{\overset{n}{\mathrm{\Σ}}}(E_{P_i}/\stackrel{\‾}{{\mathrm{\η}}_i})}\\ =1-\frac{\underset{j=1}{\overset{f}{\mathrm{\Σ}}}{E}_{F_j}}{\underset{i=1}{\overset{p}{\mathrm{\Σ}}}(E_{P_i}/\stackrel{\‾}{{\mathrm{\η}}_i})}\end{array}---\left(7\right)$

$\begin{array}{c}\stackrel{\‾}{{\mathrm{\η}}_i}=\frac{E_{P_{1,i}}+E_{P_{2,i}}...+E_{P_{j,i}}...+E_{P_{f,i}}}{E_{F_{1,i}}+E_{F_{2,i}}...+E_{F_{j,i}}...+E_{F_{f,i}}}\\ =\frac{E_{P_{1,i}}+E_{P_{2,i}}...+E_{P_{j,i}}...+E_{P_{f,i}}}{E_{P_{1,i}}/{\mathrm{\η}}_{1,i}+E_{P_{2,i}}/{\mathrm{\η}}_{2,i}...+E_{P_{j,i}}/{\mathrm{\η}}_{j,i}...+E_{P_{f,i}}/{\mathrm{\η}}_{f,i}}\\ =\frac{\underset{j=1}{\overset{f}{\mathrm{\Σ}}}{E}_{P_{j,i}}}{\underset{j=1}{\overset{f}{\mathrm{\Σ}}}(E_{P_{j,i}}/{\mathrm{\η}}_{j,i})}\end{array}---\left(8\right)$

In formula, E_mfeAnd E_refRepresent multifunctional energy resource system and the Lower heat value amount of reference system input thereof respectively (MW), wherein WithRepresent the product i of energy mix system respectively The Lower heat value amount (MW) corresponding with raw material j, and the thermal efficiency (%) of reference system；WithPoint Do not represent in sub-per unit area yield system the product during raw material j to product i, the Lower heat value amount (MW) of raw material and The thermal efficiency (%) of its process.

Claims (28)

1. one kind with low-order coal and biomass for Material synthesis methane and the method for petrol and diesel oil, it is characterised in that described Method includes:

(1) low-order coal coking is processed, obtain solid product semicoke and gas-phase product, wherein gas-phase product is separated Go out pyrolysis gas and tar；

(2) the solid product semicoke of step (1) is carried out gasification and obtain char Gasification synthesis gas；

(3) biomass gasified synthesis gas is obtained by after gasification of biomass；Described biomass and low-order coal dry ash free basis Mass ratio is 0.50～1.5；

(4) by the pyrolysis gas of step (1), the char Gasification synthesis gas of step (2) and the biomass of step (3) Carry out fischer-tropsch reaction after gasification synthesis gas mixing, then the Oil-gas Separation obtained is respectively obtained artificial oil and unconverted gas Body；The condition of described fischer-tropsch reaction is: temperature 310-370 DEG C, and catalyst is Ru/TiO₂, Co/Zr/SiO₂Or Co/MgO/SiO₂；

(5) tar that artificial oil step (4) obtained obtains with step (1) mixes, and enters hydro carbons recovery Column distillation respectively obtain temperature less than 180 DEG C, 180-320 DEG C and more than the fraction of 320 DEG C；By the temperature in described fraction Degree carries out hydrofinishing less than the fraction of 180 DEG C and 180-320 DEG C；Fraction more than 320 DEG C is hydrocracked；

The most hydrorefined reaction condition be catalyst be SiO₂-Al₂O₃Type catalyst, pressure 35-65atm, temperature 350-500 DEG C, hydrogen/oil mol ratio 5-10:1；Then cut by fraction and collect the carbon that described hydrofinishing obtains respectively Atomic number lighter hydrocarbons within 4, carbon number be the component of 5-6, carbon number be the component of 7-12, carbon atom Number is the component of 13-20；

Wherein carbon number is that the component of 5-6 carries out isomerization as auxiliary agent to improve the octane number of gasoline；Isomerization Reaction condition be catalyst be B₂O₃-Al₂O₃Type catalyst, pressure 30-40atm, temperature 320-450 DEG C, hydrogen oil rubs You compare 5-10:1；

Wherein carbon number is that the component of 7-12 carries out hydrogenation type catalytic reforming reaction as auxiliary agent to improve the pungent of gasoline Alkane value；Catalytic reforming reaction condition be catalyst be Pt/L-type zeolite catalyst, pressure 30-40atm, temperature 350-500 DEG C, hydrogen/oil mol ratio 5-10:1；

Wherein carbon number is that the component of 13-20 is as diesel oil head product；

Hydrocracking reaction condition is with magnesium silicate molecular sieve as catalyst, pressure 35-65atm, temperature 400-600 DEG C, Hydrogen/oil mol ratio 8-15:1；Isocrackate is divided into four strands: 1) carbon number lighter hydrocarbons gas within 4；2) carbon Atomic number is component and the component that carbon number is 5-6 of the temperature cut fraction hydrogenation process generation less than 180 DEG C of 5-6 Carrying out isomerization after mixing, isomerization reaction condition is consistent with above-mentioned isomerization；3) carbon number is the group of 13-20 Divide directly as diesel oil head product；4) remaining component carries out non-hydrogenation catalyst reformation；In non-hydrogenation catalyst reforming process The alkane isomerization production reformation body alkane of only 60%～80% is in order to increase octane number, and catalytic reforming condition is ZSM-5 type catalyst, pressure 25-45atm, temperature 300-500 DEG C；

(6) by after the unconverted gas mixing of the carbon number of step (5) lighter hydrocarbons within 4 and step (4) Being pressurized to 25atm for synthesizing methane, wherein, after mixing, gaseous mixture includes following percent by volume composition: CO: 15～25%, H₂: 20～30%, CO₂: 30～40%, CH₄: 7.0～15%, C₂H₆: 5.0～10%, C₂H₄: 3.0～5.0%, C₃H₈: 2.0～4.0%, C₃H₁₀: 1.0～3.0%, C₄H₁₀: 0.5～2%, C₄H₈: 0.5～2%.

Method the most according to claim 1, it is characterised in that step (1) be by after low-order coal pretreatment again Carry out coking process.

Method the most according to claim 2, it is characterised in that step (1) described pretreatment is by low-order coal Grind and be sized to the granule that particle diameter is 80-400mm, then be dried to humidity less than 8%.

Method the most according to claim 1, it is characterised in that the coking of step (1) process be at air and Carry out in the presence of middle pressure steam.

Method the most according to claim 4, it is characterised in that step (1) medium pressure steam is that pressure exists The steam of 25atm.

Method the most according to claim 4, it is characterised in that it is in ferrum system that step (1) described coking processes Carry out in the presence of oxide.

Method the most according to claim 6, it is characterised in that the reaction temperature that step (1) described coking processes Degree is 400 DEG C～600 DEG C, pressure 25atm.

Method the most according to claim 6, it is characterised in that step (1) described ferrous oxide is FeO_x And Fe₂O₃In the mixing of one or more.

Method the most according to claim 8, it is characterised in that step (1) described FeO_xFor FeO.

Method the most according to claim 1, it is characterised in that step (1) obtain solid product semicoke and After gas-phase product, wherein by gas-phase product through solid impurity separating treatment, then isolate pyrolysis gas and tar.

11. methods according to claim 1, it is characterised in that step (2) is by the solid of step (1) Product semicoke carries out gasification in the presence of oxygen gas and water and high steam and obtains char Gasification synthesis gas.

12. methods according to claim 11, it is characterised in that the high steam described in step (2) is pressure The steam of power 40atm.

13. methods according to claim 1, it is characterised in that step (4) is by the pyrolysis of step (1) After the biomass gasified synthesis gas mixing of gas, the char Gasification synthesis gas of step (2) and step (3) by gaseous mixture first Fischer-tropsch reaction is carried out again through CO transformationreation.

14. methods according to claim 13, it is characterised in that step (4) is after CO transformationreation The H of gaseous mixture₂The mol ratio of/CO is 1.3-2.4.

15. methods according to claim 14, it is characterised in that step (4) is after CO transformationreation The H of gaseous mixture₂The mol ratio of/CO is 1.5.

16. methods according to claim 13, it is characterised in that gaseous mixture is become by step (4) through CO After changing reaction, by gaseous mixture through NHD solvent absorption, then carry out fischer-tropsch reaction.

17. methods according to claim 13, it is characterised in that step (4) is by the CO in gaseous mixture₂ And H₂S content is removed to 500ppm and below 25ppm respectively, then carries out fischer-tropsch reaction.

18. methods according to claim 1, it is characterised in that be by Jiao of step (1) in step (5) Oil hydrotreating, then the artificial oil obtained with step (4) carries out common refining.

19. methods according to claim 18, it is characterised in that step (5) is by the tar of step (1) After hydrotreating, the H/C mol ratio of tar increases to 0.7-1.2.

20. methods according to claim 18, it is characterised in that step (5) is by the tar of step (1) The reaction condition of hydrotreating be catalyst be FeS-Fe₂O₃Type catalyst, pressure 30-40atm, temperature 250-350 ℃。

21. methods according to claim 1, it is characterised in that in step (6), the carbon by step (5) is former Pre-methanation resynthesis methane is first carried out after the unconverted gas mixing of subnumber lighter hydrocarbons within 4 and step (4).

22. methods according to claim 21, it is characterised in that step (6) is by former for the carbon of step (5) CO is first carried out after the unconverted gas mixing of subnumber lighter hydrocarbons within 4 and step (4)₂Membrance separation, then by pre- The lighter hydrocarbons of carbon number more than 2 are converted into synthesis gas by methanation reaction, then synthesizing methane.

23. methods according to claim 22, it is characterised in that step (6) carries out CO₂After membrance separation CO in gas₂Percent by volume is less than 2.0%.

24. methods according to claim 22, it is characterised in that the reaction condition of step (6) pre-methanation Be catalyst be SiO₂Type catalyst, pressure 20-30atm, temperature 400-500 DEG C.

25. 1 kinds of low-order coal and the system that biomass are Material synthesis methane and petrol and diesel oil, it is characterised in that described system System includes: low-order coal pretreatment unit (1), low-order coal cracking units (2), solid impurity separator (3), coal tar Recovery of oil equipment (4), air-separating plant (5), char Gasification unit (6), biomass pretreatment unit (7), Gasification of biomass unit (8), synthesis gas blender (9), synthesis gas CO shift-converter (10), synthesis gas are clean Change unit (11), Fischer-Tropsch synthesis device (12), oil gas diverter (13), oil product refine unit (14) altogether, former Material gas blender (15), CO₂Membrane separation plant (16), pre-methanator (17), methanator (18)； Wherein low-order coal pretreatment unit (1) is connected with low-order coal cracking units (2), in low-order coal cracking units (2) The gas-phase product obtained passes sequentially through solid impurity separator (3) and coal tar recovering equipment (4), coal tar recovering Equipment (4) is refined unit (14) altogether and is connected with oil product, the solid product obtained in low-order coal cracking units (2) half Jiao is transported to char Gasification unit (6)；Biomass are transported to biomass through biomass pretreatment unit (7) Gasification unit (8)；Air is passed through char Gasification unit (6) through air-separating plant (5) isolated oxygen, Char Gasification unit (6), gasification of biomass unit (8) and coal tar recovering equipment (4) mix with synthesis gas respectively Device (9) connects so that from the pyrolysis gas of coal tar recovering equipment (4), from char Gasification unit (6) Char Gasification synthesis gas and from the biomass gasified synthesis gas of gasification of biomass unit (8) in synthesis gas blender (9) Middle mixing, synthesis gas blender (9) downstream successively with CO shift-converter (10), purified synthesis gas unit (11), Fischer-Tropsch synthesis device (12) and oil gas diverter (13) connect；Two outlets of oil gas diverter (13) are respectively Refine unit (14) with oil product altogether and unstripped gas blender (15) is connected；Oil product refines of unit (14) altogether Outlet is connected with unstripped gas blender (15) so that oil gas diverter (13) unconverted gas out refines altogether with oil product The carbon number of unit processed (14) lighter hydrocarbons within 4 sequentially pass through after unstripped gas blender (15) mixes again CO₂Membrane separation plant (16), pre-methanator (17) enter into methanator (18).

26. systems according to claim 25, it is characterised in that described low-order coal cracking units (2) is solid Fixed bed reactor.

27. systems according to claim 25, it is characterised in that described char Gasification unit (6) is slurry stream Bed gasification furnace.

28. systems according to claim 25, it is characterised in that described gasification of biomass unit (8) is stream Change bed gasification furnace.