CN105142769A - System for making renewable fuels - Google Patents

Abstract

Multiple catalytic processing stations coupled with a system which produces volatile gas streams from biomass decomposition at discrete increasing temperatures or constant temperature. These catalytic processing stations can be programmed to maximize conversion of biomass to jet fuel components. The system may also include a processing station for subjecting biomass within the stations to at least one programmable starting temperature (T start) and for incrementing an individual processing station temperature by programmable increments (delta T) to produce a volatile and a non-volatile component. Further, methods for converting biomass and char to renewable jet fuel, diesel, and kerosene are disclosed.

Description

For the production of the system of recyclable fuel comprising gasoline, diesel oil and jet fuel

related application

This application claims on December 7th, 2012 submit to No. PCT/US2012/068616th, PCT application priority and be its partial continuous application, No. PCT/US2012/068616th, PCT application requires the priority of No. 13/361828th, the U. S. application (existing No. 8383049th, United States Patent (USP)) of No. 13/361840th, U. S. application (existing No. 8431757th, United States Patent (USP)) and the submission on January 30th, 2012 submitted on January 30th, 2012, and its full content is incorporated to herein by reference.This application also requires the priority of No. 61/691713rd, the U.S. Provisional Application submitted on August 21st, 2012, and its full content is incorporated to herein by reference.

Technical field

The present invention relates generally to the system for the manufacture of recyclable fuel, and relate more specifically to utilize optionally programmable system, by a series of catalyst, biomass thermal is chemically converted into recyclable fuel and other useful chemical compound, comprises gasoline, diesel oil and jet fuel.

Background technology

The fossil fuel resource continuing through its preciousness along with the world runs, and it will be forced to turn to other energy.Current universal goal comprises cheap and obtains energy rapidly.Through the ages, the mankind have turned to living beings to be provided the energy of hot aspect by burn wood and other biological matter.This is a kind of process of very poor efficiency in essence.Burning can be made more effective by introducing programmability.It is similar to the building being incorporated into by computer and needing to carry out heating.Just heat this building in order to only have when people occurs, place in this building when sensor detects people with convenient sensor and connect heater.This is an example of programmable system.Similarly, the chemical bond rupture of programmable system for causing biomass efficient to change into high value added product can being introduced, wherein, only having the bond fission of minimal amount, therefore, expend the energy of minimum for these keys that rupture.

The importance of bond fission and industrial useful product (as gasoline and the diesel oil) that forms that to be biomass conversion be.Various forms of laboratory and on a small scale commercial biomass pyrolytic device have developed into and have generated useful chemical products from the controlled thermolysis of biomaterial (from wood chip to sewage sludge).Although some pyrolysis apparatus focus only on production synthesis gas, in the relatively mild pyrolytical condition of exploitation, there is sizable effort, this causes the condensate liquid being called as bio oil or pyrolysis oil usually.With the example that the programmable system that the pyrolytical condition of gentleness operates can be effective bond fission and formation.On laboratory level, develop the pyrolysis apparatus of many forms to produce the intermediate compound that these are referred to as bio oil or pyrolysis oil.Configuration comprise various forms of fluidized bed pyrolyzer that the simple tube furnace, the wherein timber that wherein toast living beings in ceramic ship mixes with hot sand relative to ablation pyrolysis apparatus, wherein living beings that hot surface rubs and various design based on early stage coking furnace more simply configure.

The basic problem of gained pyrolysis oil is that it is made up of to allow thousands of compounds hundreds of, and this is the result making the far-ranging temperature of the large quantities of experience of unprocessed living beings, time and pressure distribution.When this process becomes complexity due to the thousands of primary biological compound in primitive organism raw material, result is large quantities of almost thorny all gained compounds mixed.The pyrolysis oil that such method obtains is not thermodynamically stable usually.They comprise the active oxygen radical by organic acid and base catalysis, thus make these oil usually last several days to develop into dark mixture from light color liquid, be entrained with tar and resinous substances in this mixture.In addition, attempt again gasification and pyrolysis oil and usually can cause extra chemical reaction, this produces extra biological coke and causes changing into the lower-molecular-weight component in gained gas flow.Although can realize the quite high productive rate of pyrolysis oil in laboratory scale test, large plant-scale demonstrative project can produce much lower productive rate usually.This is the temperature of more wide region in the three-D volumes of the much bigger heating of framework due to this increase, retention time and local pressure by inference.

To catalyst system and catalyzing introduce programmable adaptive previously made great efforts to comprise set up several parallel connection reactor (being similar to microprocessor bus) to study the Gehrer design of catalytic gas reaction.(JournalofPhysicsE:ScientificInstruments18(1985)836)。The United States Patent (USP) 6994827 of the people such as the United States Patent (USP) 6548026 of the people such as Dales and Safir discloses the parallel reactor able to programme that can control container mixing speed, temperature and pressure.In addition, the U.S. Patent application 2010/0223839 of the people such as Garcia-Perez discloses heating biological matter to the first temperature, its objective is the follow-up anhydrousugar content improving and develop in the oily portion of biomass pyrolysis product.Object is the fermentability in order to improve the oily portion for alcohol production subsequently.This is the example of some programmable systems for biomass conversion.

Summary of the invention

The embodiment of the application is provided for biomass conversion being the system and method for recyclable fuel, any combustible fuel being meant to biomass derived of recyclable fuel.Recyclable fuel may be used for transport, heating or other objects, and may be used for the preparation of these fuel of such as gasoline, diesel oil, jet fuel, kerosene or other useful blending of fuel things (admixture (BTX) as benzene, toluene and dimethylbenzene), fusion or formation.

Embodiments more of the present invention relate to the system and method for creating optionally technique able to programme, and the chemical compound that biomass derived decomposes in the process is sent to different Catalytic processes to produce the product containing recyclable fuel and other value-added product.

Further embodiment of the present invention for a kind of for biomass pyrolysis product being changed into useful chemical substance and the efficient system of recyclable fuel.

Other embodiments for a kind of temperature correlation with the devolatilization of living beings, for extracting the technique of the energy of maximum from the living beings for changing into gasoline or diesel oil.

Another embodiment of the invention relate to a kind of relevant to the load balance that the catalyst under specified temp exports, for extracting the technique of the energy of maximum in the living beings from the gasoline for changing into or diesel oil.

In further embodiment, the present invention is directed to the system becoming diesel oil or jet fuel for biomass conversion, it comprises: the device comprising multiple treatment bench (N) (processingstation) and a series of catalyst; Each treatment bench can apply at least one initial temperature (T to the living beings in platform _start) to produce volatility and nonvolatile element; At least one catalytic reactor (catalystreactor) is for being received in the volatile ingredient produced in each treatment bench; Wherein, at least one catalytic reactor described comprises the catalyst being selected from dehydration catalyst, olefin oligomerization catalyst and hydrotreating catalyst.

In another embodiment, this system comprises extra catalytic reactor.

In still another embodiment, series connection uses extra catalytic reactor.

In still another embodiment, the catalytic reactor that use in parallel is extra.

In still another embodiment, this system comprises the temperature controller for being increased progressively independent treatment bench temperature by increment (Δ Τ).

In another embodiment, nonvolatile element is carbonaceous material.

In embodiments, this system also comprises the gasifier for converting carbonaceous material being become synthesis gas.

In embodiments, this system also comprises the conduit for introducing synthesis gas from gasifier to catalytic reactor.

In embodiments, this system also comprises the treatment bench quantity (N) of 2 to 1000, and wherein T _{open begin}in the scope of 100 DEG C to 1000 DEG C.In addition, temperature increment (Δ Τ) is in the scope of 0 DEG C to 200 DEG C.

In another embodiment, this system also comprises for holding co-fed reservoir, with for by the co-fed conduit be incorporated in volatile component or at least one treatment bench, wherein, be describedly co-fedly selected from alcohols, aldehydes, ketone, ethers, carboxylic acids and hydro carbons.

In another embodiment, this system comprises the conduit from gasifier to the catalytic reactor containing syngas conversion catalyst, wherein, describedly co-fedly to be produced by syngas conversion catalyst.

In another embodiment, described living beings are selected from lipid, hemicellulose, cellulose and lignin.

In still another embodiment, described living beings are selected from two kinds of lipid, hemicellulose, cellulose and lignin or the mixture of more kinds of living beings.

In further embodiment, according to the type selecting T in the mixture of two kinds or more kinds of living beings with the living beings of maximum concentration _start.In another embodiment, at least 2 treatment benches are set as identical T _start.In another embodiment, all treatment benches are set as identical T _start.In another embodiment, T _startit is the temperature of substantial constant.In another embodiment, nonvolatile element is heat conduction.In another embodiment, the nonvolatile element of N number for the treatment of bench comprises coke.

In still another embodiment, N number for the treatment of bench comprises the input of fuel gas that can accept recirculated water that external water source, carbon dioxide or methane or inside provides or be caused by catalyst treatment.

In another embodiment, dehydration catalyst comprises the combination of any acid catalyst or acid catalyst.In still another embodiment, olefin oligomerization catalyst is dehydration catalyst.

In another embodiment, this system also comprises conduit with the water will produced in system, carbon dioxide and methyl alcohol guiding gasifier for the conversion of nonvolatile element to synthesis gas.

In another embodiment, the raw material for next platform is comprised from the nonvolatile element of platform.

In another embodiment, the diesel oil of generation or jet fuel comprise one or more kerosene component.In another embodiment, wherein, the diesel oil of generation or jet fuel comprise one or more jet fuel components.In another embodiment, the diesel oil of generation or jet fuel comprise one or more diesel fuel constituents.

In another embodiment, the water generated inside, carbon dioxide, methyl alcohol are used as described carbonaceous material to the reactant in the conversion of synthesis gas.

In still another embodiment, treatment bench is selected from pyrolysis reactor, fixed bed reactors, fluidized-bed reactor, circulating bed reactor, bubbling fluidization bed bioreactor, vacuum moving-burden bed reactor, drainage type reactor, cyclonic reactor, vortex reactor, rotating cone reactor, helical reactors (augerreactor), ablation reactor, the pyrolysis reactor of microwave radiation technology, the pyrolysis reactor of plasmaassisted, the chamber in living beings fractionating system, gasifier and vacuum moving-burden bed reactor.

In embodiments, the present invention includes the system for coke being become recyclable fuel, it comprises: the device comprising multiple treatment bench (N) and a series of catalyst; Each treatment bench can make the coke in platform experience at least one initial temperature (T _start) to produce synthesis gas; For being received at least one catalytic reactor of the synthesis gas produced in each treatment bench; Wherein, at least one catalytic reactor described comprises the catalyst being selected from syngas conversion catalyst, methanol synthesis catalyst, DME synthetic catalyst, dehydration catalyst, olefin oligomerization catalyst and hydrotreating catalyst.In another embodiment, this system comprises extra catalytic reactor.These extra catalytic reactors can use by serial or parallel connection.

In another embodiment, treatment bench is selected from pyrolysis reactor, fixed bed reactors, fluidized-bed reactor, circulating bed reactor, bubbling fluidization bed bioreactor, vacuum moving-burden bed reactor, drainage type reactor, cyclonic reactor, vortex reactor, rotating cone reactor, helical reactors, ablation reactor, the pyrolysis reactor of microwave radiation technology, the pyrolysis reactor of plasmaassisted, the chamber in living beings fractionating system, gasifier and vacuum moving-burden bed reactor.

Another embodiment relates to the method for by biomass conversion being diesel oil or jet fuel, comprising: living beings are assigned to multiple treatment bench (N); The living beings in platform are made to experience at least one initial temperature (T _{open begin}) to produce volatility and nonvolatile element; Described volatile component is imported at least one catalytic reactor, and described at least one catalytic reactor designs becomes to implement to be selected from one or more techniques of dehydration, olefin(e) oligomerization and hydrotreatment; Be collected in the diesel oil or jet fuel that produce at least one catalytic reactor described.

Further embodiment comprises the method for coke being become diesel oil or jet fuel, comprising: coke is assigned to multiple treatment bench (N); Make the coke in platform experience at least one and start temperature (T _start) to produce synthesis gas; Described synthesis gas is imported at least one catalytic reactor, and described at least one catalytic reactor designs becomes to implement to be selected from one or more techniques of Synthetic holography catalysis, methanol synthesis catalyst, DME synthesis catalytic, dehydration, olefin(e) oligomerization and hydrotreatment; Be collected in the diesel oil or jet fuel that produce at least one catalytic reactor described.

In another embodiment, the method also comprises extra catalytic reactor.In another embodiment, extra catalytic reactor series connection uses.In another embodiment, extra catalytic reactor parallel connection uses.

In the further embodiment of the method, treatment bench is selected from pyrolysis reactor, fixed bed reactors, fluidized-bed reactor, circulating bed reactor, bubbling fluidization bed bioreactor, vacuum moving-burden bed reactor, drainage type reactor, cyclonic reactor, vortex reactor, rotating cone reactor, helical reactors, ablation reactor, the pyrolysis reactor of microwave radiation technology, the pyrolysis reactor of plasmaassisted, the chamber in living beings fractionating system, gasifier and vacuum moving-burden bed reactor.

In another embodiment, the method uses the temperature controller being used for being increased progressively independent treatment bench temperature by increment (Δ Τ).In still another embodiment, the quantity (N) for the treatment of bench is in the scope of 2 to 1000, and wherein T _startin the scope of 100 DEG C to 1000 DEG C.In another embodiment, temperature increment (Δ Τ) is in the scope of 0 DEG C to 200 DEG C.

Can find other characteristic sum aspects of the present invention from the detailed description of making below in conjunction with accompanying drawing significantly, accompanying drawing is by embodiment, according to the feature of embodiment of the present invention.This general introduction is not intended to limit the scope of the invention, and it is limited only by the accompanying claims.

Accompanying drawing explanation

According to one or more various embodiment, describe the present invention in detail with reference to the following drawings.There is provided accompanying drawing only for illustration of object and typical case of the present invention or example embodiment are only described.There is provided these accompanying drawings so that reader understanding the present invention and should not think to limit range of the present invention, scope or applicability.It should be noted that these accompanying drawings are not necessarily drawn in proportion in order to know and be convenient to illustrate.

Fig. 1 is the figure of the N number for the treatment of bench illustrated on runway (racetrack), and wherein, each treatment bench runs at a certain temperature.

Fig. 2 is according to one or more embodiments of the present invention, for generation of the detail flowchart of the optionally programmable catalysis chain of recyclable fuel.

Fig. 3 is in one or more embodiment of the present invention, and the flow chart of the optionally programmable catalysis chain with three platforms is shown, these three platforms be configured to process there is different composition enter living beings.

Fig. 4 is according to one or more embodiment, is applied to the flow chart of the optionally programmable catalysis chain of regeneration jet fuel, kerosene and the diesel fuel produced except gasoline.

Fig. 5 is according to one or more embodiment, is applied to the flow chart of the programmable catalysis chain of regeneration jet fuel, kerosene and the diesel fuel produced except gasoline.

Fig. 6 is the flow chart that principle according to the present invention describes a kind of algorithm, and this algorithm depends on and increases progressively treatment bench temperature until reach desired maximum temperature.

Fig. 7 is the flow chart that principle according to the present invention describes a kind of algorithm, and this algorithm depends on the Differential Output of various catalysis chain.

Fig. 8 A is the figure that the fuel of the sunflower seeds utilizing dehydration catalyst, aromatized catalyst, gas modifying catalyst (gas-upgradingcatalyst) exports relative to temperature; Fig. 8 B illustrates that A shunting (after dehydration catalyst) exports relative to the comparison of U.S. diesel oil #2 and biodiesel B99; And Fig. 8 C and 8D the gentle body modifying catalyst of aromatized catalyst is shown after gas-chromatography (GC) data of recyclable fuel that obtain.

Fig. 9 is GC figure red fir (redfir) being used as the escaping gas that input living beings are collected after aromatized catalyst.

These figure are not intended to be limit or to limit the invention to disclosed precise forms.Should be appreciated that the present invention can implement with amendment and distortion, and the present invention is only subject to the restriction of claims and equivalents thereof.

Specific embodiments

In one embodiment of the invention, a kind of system for system conveying (routing) biomass decomposition product by being made up for the treatment of bench and a series of catalyst is described.In one embodiment, achieve optionally programmable system to maximize for making the output of pyrolysis system.This optionally programmable system there are three kinds of basic skills: a) based on the route (routing) of the understanding of the initial composition to living beings, b) based on the route of the understanding of the temperature of the devolatilization to living beings, with c) based on the route of load balance.Whole character of these methods will be described now by referring to accompanying drawing.

Method living beings being introduced treatment bench comprises to be introduced by conveyer belt, hopper and/or pulverizer.Treatment bench can provide in the pulverizing of living beings and/or pyrolysis one or both.Treatment bench described herein can comprise encapsulating these assemblies in a system, wherein such as, pulverizes and is closely connected with cracking assembly.Can in original form or dried forms introduce living beings, or can work as pyrolysis start time in pyrolysis chamber drying.

As used herein, term " living beings " comprises any material deriving from plant origin or easily obtain.This material can include but not limited to: (i) plant product, such as bark, leaf, branch, stub, hardwood sheet, cork sheet, grape float stone (grapepumice), bagasse, switchgrass; (ii) such as grass, timber and the pellet of hay pellet or the material of chopping, the crop product of such as corn, wheat and mestha.This term can also comprise seed, such as vegetable seeds, fruit seeds and seeds of leguminous plant.

Term " living beings " can also comprise: (i) drains product, comprises animal wastes, and Tathagata is from the excreta of poultry; (ii) business or recycled materials, comprise plastics, paper, paper pulp, cardboard, sawdust, wood residues, wooden shavings and cloth; (iii) municipal refuse of sewage waste is comprised; (iv) agricultural wastes, such as cocoanut shell, pecan shell, Pericarppium Armeniacae Amarum, coffee grounds; (v) agriculture feed product, such as straw, wheat straw, rice husk, corn stalk, maize straw and corncob.The various compounds of classifying in the classification of living beings typically by cellulose, hemicellulose, lignin, starch and lipid form.Living beings also can be made up of plant residue, seed residue and seed expelleers oily (material remaining after extracting oil from seed).

With reference to Fig. 1, a series of N number for the treatment of bench 50 is sequentially arranged around quadrangle track 52.Treatment bench 50 can comprise any amount of known pyrolysis reactor, comprises fixed bed reactors, fluidized-bed reactor, circulating bed reactor, bubbling fluidization bed bioreactor, vacuum moving-burden bed reactor, drainage type reactor, vortex or vortex reactor, rotating cone reactor, helical reactors, ablation reactor, the pyrolysis reactor of microwave or plasmaassisted and vacuum moving-burden bed reactor.It can also comprise the chamber in living beings fractionating system described in the U.S. Patent Publication the 2010/0180805th (being now United States Patent (USP) 8216430) as owned together, and its full content is incorporated to herein by reference.

In any one time, each treatment bench 50 (is labeled as T on each treatment bench side in FIG in certain temperature ₁... T _n) under run.Therefore, the first treatment bench is at T ₁the platform 1 of lower operation and the N number of is at temperature T _n-lower operation.Each treatment bench 50 can run at any temperature being equal to or higher than previous treatment bench.Initiated process platform temperature is normally determined by the initial composition of living beings.This device holds N number for the treatment of bench altogether, and wherein N can be adjusted to 1000 by operator from 2, preferably between 2 and 100, and most preferably between 2 and 50.Can increase progressively platform temperature by variable delta Δ Τ, variable delta Δ Τ can in the scope of 0 DEG C to 200 DEG C.In one embodiment, all treatment benches 50 run at that same temperature.In another embodiment, each follow-up treatment bench temperature is than previous treatment bench incrementally high Δ Τ.In still another embodiment, one group of adjacent treatment bench runs under identical temperature T, then be that another that run under temperature T+x* Δ Τ organizes adjacent treatment bench, then be then run under temperature T+y* Δ Τ another group treatment bench, wherein x and y be more than or equal to 1 any number.In further embodiment, temperature increment is by realizing with applying thermograde to living beings under applying to exist at compression shock.Describe in detail this technology in the U.S. Patent application 13/019236 (present United States Patent (USP) 8293958) of CO-PENDING and U.S. Patent application 13/103905 (present United States Patent (USP) 8367881), its full content is incorporated to herein by reference.

During heating, treatment bench 50 produces volatility and nonvolatile element.Because this material in relatively narrow temperature range and can heat in seclected time, involatile constituent (partly to form the form of coke) has embedding extra volatile ingredient wherein, its be extractible and as the time expand such as under selected temperature or the result that is exposed at higher temperature processed in follow-up treatment bench.In some embodiments, single biomass samples steps to treatment bench from treatment bench, under each treatment bench is in identical temperature.Cause the extra time under selected temperature extracting extra volatile component at each place.In some embodiments, single biomass samples steps to treatment bench from treatment bench, under each treatment bench is in the temperature than previous Tai Genggao.Cause the extra time under selected temperature extracting extra volatile component at each place.In other embodiments, each comprises different biomass samples.For treating that the specific living beings of pyrolysis optimize time and the temperature of pyrolysis.

Therefore, the different volatile component formed can be had to obtain by operational processes platform in a number of different ways.The output of these treatment benches is connected with a series of catalyst as described below.

The various compounds of classifying in the classification of living beings typically by cellulose, hemicellulose, lignin, starch and lipid form.When experiencing pyrolytic process, these compounds are through the decomposition of multiple step.Such as, hemicellulose contains C5 sugar, such as fructose and wood sugar, produces furfural and hydroxymethylfurfural during its pyrolysis.The latter's compound can be further converted to fuel intermediate product furans and oxolane.In treatment bench 50, the relatively narrow temperature window of experience allows to collect these useful intermediates.

Fig. 2 depicts the embodiment with eight treatment benches 50 and a series of catalyst channels, and this series of catalyst channels comprises dehydration catalyst 60, the gentle body modifying catalyst 62 of aromatized catalyst 61.During cooling, the output of each catalytic arrays is made up of escaping gas (under chilling temperature), recyclable fuel and water.Then escaping gas is by follow-up catalysis post.Depend on temperature and the living beings composition for the treatment of bench 50, use selector switch 55,56,57 can make to be transmitted by one or more catalyst 60,61,62 from the volatile component of any given treatment bench.In some embodiments, the volatile component from multiple treatment bench can be merged and use selector switch 55,56,57 that the volatile component of merging can be made to be transmitted by one or more catalyst 60,61,62.Line 21 illustrates and can join in aromatized catalyst 61 as extra charging using optional cosolvent, and it can contribute to the productive rate improving liquid fuel component.Cosolvent can from typical synthesis gas converter 64 in-situ preparation.Carbon monoxide for the synthesis of gas converter (for generation of cosolvent) and hydrogen can be obtained by known reaction (such as, utilizing the carbon solid stayed of the pyrolysis from living beings in treatment bench 50) or other known methods.Cosolvent can comprise oxygenatedchemicals, such as aldehyde, alcohol, ketone, ether and carboxylate, and hydrocarbon.In other embodiments, cosolvent can obtain from commercial source.

If the volatile component from treatment bench 50 be chosen as through dehydration catalyst 60, then output is by room temperature separator 32, and output is separated into water, recyclable fuel 33 and escaping gas 34 by it.Then escaping gas is conducted through aromatized catalyst 61 to produce a kind of product, this product by the cooling of cold separator 35 (such as, at a temperature below the room temperature) produce water, recyclable fuel 36 and escaping gas 37, it can comprise fuel gas 41, such as, compound containing C1-C5.Then these fuel gas can be discharged via variable relief valve 58.The route that variable relief valve can control escaping gas 37 is to gas modifying catalyst room or fuel gas treatment facility (plant), or to both.After being cooled by cold separator 38, the product from gas modifying catalyst 62 produces water, recyclable fuel 39 and escaping gas 40, and it can comprise combustible gas mixture 42.This combustible gas mixture both can process or be recycled to aromatized catalyst room via recirculation pump 59 in fuel gas treatment facility.In another embodiment, combustible gas mixture 42 can be recycled to following in one or more: (a) at least one or more treatment bench 50, (b) dehydration catalyst 60, (c) aromatized catalyst 61, and (d) gas modifying catalyst 62.

Fig. 3 illustrates embodiment 300, and embodiment 300 utilizes and transforms various types of biomass material to obtain optimum Product yields to understanding three treatment benches 50 of the initial composition of living beings and row's catalysis post.Biomass material in each can from the single living beings charging (input) utilizing described three platform process, or from the charging of multiple independently living beings.Although the number for the treatment of bench can change, identical catalysis post is used for escaping gas to be converted into recyclable fuel.Wherein the order of selective catalysis post can change.

In one or more embodiment, First comprises the living beings (A) being rich in lipid.Although this figure shows only use a platform, be appreciated that to use and be in multiple workbench under identical or different temperatures to produce volatile component.When with when being rich in living beings (A) charging of lipid, platform 1 produces the product comprising escaping gas and carbon solid.Platform 1 preferably runs at lower than 300 DEG C.Volatile component by dehydration catalyst 60 to produce the first product.Room temperature trap (roomtemperaturetrap) is used to cool this first product and this first product is made up of water, the first recyclable fuel (its under collection condition normally liquid) and the second volatile ingredient.Then the first recyclable fuel is reclaimed.Dehydration catalyst runs under the pressure being less than 2 bar, preferably in the temperature range of 400-700 DEG C, most preferably in the scope of 400 DEG C to 500 DEG C, and is used for recycle-water from escaping gas.

Dehydration catalyst 60 can be any acid catalyst.The acid catalyst being applicable to the application is heterogeneous (or solid) acid catalyst.Can at least one catalyst carrier this at least one solid acid catalyst (being referred to herein as Supported heteropoly acid catalyst) of load.Solid acid catalyst comprises, but be not limited to, (1) heterogeneous heteropoly acid (HPAs) and their salt, (2) natural clay mineral matter, such as containing those of aluminium oxide or silica (comprising zeolite), (3) cationic ion-exchange resin, (4) metal oxide, (5) metal oxide mixed, (6) from these sour derivative inorganic acid or slaine, such as metal sulfide, metal sulfate, metal sulfonate, metal nitrate, metal phosphate, metal phosphinate hydrochlorate, metal molybdate, metal tungstates, metal borate, (7) combination of 1 to 6 is organized.

Suitable HPAs comprises and has general formula X _am _bo _c ^q-compound, wherein, X is hetero atom, such as phosphorus, silicon, boron, aluminium, germanium, titanium, zirconium, cerium, cobalt or chromium, and M is at least one transition metal, such as tungsten, molybdenum, niobium, vanadium or tantalum, and q, a, b and c are the independent integer selected or its mark.Method for the preparation of HPAs is well known in the art.Natural clay mineral matter is known in the art and includes, but not limited to kaolin, bentonite, attapulgite, montmorillonite and zeolite.Suitable cationic ion-exchange resin is the strong cation-exchanging resin of styrene-based-divinyl benzene copolymer, such as (Rohm & Haas; Philadelphia, PA), (such as, monosphereM-31) (Dow; Midland, MI), from the CG resin of Resintech company (WestBerlin, NJ), and Lewatit resin, as the MonoPlusTMS100H from SybronChemicals company (Birmingham, NJ).When it is present, the metal component of group 4 to 6 can be selected from the element of race I, Ila, Ilia, Vila, Villa, lb and lib from the periodic table of elements and aluminium, chromium, tin, titanium and zirconium.Flurosulphonic acid polymer also can be used as the solid acid catalyst of technique disclosed herein.

Then the second volatile component is transported to aromatized catalyst 61 to produce the second product, it enriches the product in aromatic compounds.Use conversely at 0-20 DEG C, the cold-trap more preferably at 0-5 DEG C cools this second product.Output from cold-trap is made up of water, the second recyclable fuel and the 3rd volatile component.Then the second recyclable fuel is reclaimed.Under the pressure lower than 2 bar, preferably in the temperature range of 300 DEG C to 500 DEG C, most preferably at the range of operation aromatized catalyst 61 of 325 DEG C to 400 DEG C.Aromatized catalyst 61 can be made up of MFI type zeolite and metal-modified MFI type zeolite, and wherein, metal is selected from VI B race metal, VII B race metal, VIII race's metal, I B race metal, II B race metal, Ga, In and their combination.

Then the 3rd volatile component is transported to gas modifying catalyst 62 to produce third product.Use conversely at 0-20 DEG C, the cold-trap more preferably at 0-5 DEG C cools this three products.Output from cold-trap is made up of water, the 3rd recyclable fuel and the 4th volatile component.Then the 3rd recyclable fuel is reclaimed.Under the pressure lower than 2 bar, preferably in the temperature range of 400 DEG C to 700 DEG C, most preferably at the range of operation gas modifying catalyst 62 of 500 DEG C to 600 DEG C.Gas modifying catalyst 62 can be made up of metal-modified MFI type zeolite, and wherein metal is selected from Ga, Zn, In, Mo, W, Cr, Pt, Pd, Rh, Ru, Au, Ir and their combination.4th volatile component can be recycled to following at least one: a) one or more treatment bench 50, b) dehydration catalyst 60, c) aromatized catalyst 61, d) gas modifying catalyst 62, and e) fuel gas treatment facility.

Still with reference to Fig. 3, platform 2 can comprise the living beings (B) being rich in hemicellulose that derive from other biological raw material or the carbon solid from a upper platform 50, and this carbon solid is included in nonvolatile volatile component in previous.Although this figure shows only use a platform, be appreciated that to use and be in multiple workbench at identical or different temperature to produce volatile component.Platform 2 preferably higher than 300 DEG C and lower than 500 DEG C at run.Operator optionally programmably can increase progressively the temperature in (Δ Τ) platform 2.Temperature increment can preferably in the scope of 10-200 DEG C.By means of different initial biomass and/or different initial temperatures, platform 2 produces the product be made up of with the carbon solid being different from the carbon solid produced in a upper platform volatile ingredient.Then the volatile component produced in platform 2 is conducted through aromatized catalyst 61 to produce the 4th product.Then, at being used in 0-20 DEG C, the cold-trap more preferably at 0-5 DEG C cools this four-product.Then the 4th recyclable fuel is reclaimed.Output from cold-trap is made up of water, the 4th recyclable fuel and the 5th volatile component.Aromatized catalyst 61 operates and preferably in the temperature range of 300 DEG C to 500 DEG C, most preferably runs in the scope of 325 DEG C to 400 DEG C under the pressure lower than 2 bar.

Then the 5th volatile component is delivered to gas modifying catalyst 62 to produce the 5th product.At being used in 0-20 DEG C conversely, the cold-trap more preferably at 0-5 DEG C cools the 5th product.Output from cold-trap is made up of water, the 5th recyclable fuel and the 6th volatile component.Then the 5th recyclable fuel is reclaimed.Preferably in the temperature range of 400 DEG C to 700 DEG C, most preferably in the scope of 500 DEG C to 600 DEG C, this gas modifying catalyst 62 is run under the pressure lower than 2 bar.6th volatile component can be recycled to following at least one: a) one or more treatment bench 50, b) dehydration catalyst 60, c) aromatized catalyst 61, d) gas modifying catalyst 62, and e) fuel gas treatment facility.

Still with reference to Fig. 3, platform 3 runs at higher than 500 DEG C, and the carbon solid of the biomass material of lignin or the remnants from a upper platform is independently rich in process.Only use a platform although the figure shows, be appreciated that to use and be in multiple workbench at identical or different temperature to produce volatile component.By means of different initial biomass and/or different initial temperatures, platform 3 produces the product containing escaping gas and different carbon solids.Make these volatile components by dehydration catalyst 60 to produce the 6th product.Room temperature trap is utilized to cool the 6th product and the 6th product is made up of water, the 6th recyclable fuel and the 7th volatile component.Then the 6th recyclable fuel is reclaimed.Dehydration catalyst 60, under the pressure being less than 2 bar and preferably in the temperature range of 400-700 DEG C, most preferably runs in the scope of 400 DEG C to 500 DEG C.Dehydration catalyst 60 can be same as described above.

Then the 7th volatile component is transported to previously described aromatized catalyst 61 to produce the 7th product.Be used in 0-20 DEG C conversely, the cold-trap most preferably at 0-5 DEG C cools the 7th product.Output from this cold-trap is made up of water, the 7th recyclable fuel and the 8th volatile component.Then the 7th recyclable fuel is reclaimed.Under the pressure lower than 2 bar and preferably in the temperature range of 300 DEG C to 500 DEG C, most preferably at the range of operation aromatized catalyst 61 of 325 DEG C to 400 DEG C.

Then the 8th volatile component is transported to previously described gas modifying catalyst 62 to produce the 8th product.Be used in 0-20 DEG C conversely, the cold-trap most preferably at 0-5 DEG C cools the 8th product.Output from this cold-trap is made up of water, the 8th recyclable fuel and the 9th volatile component.Then the 8th recyclable fuel is reclaimed.Under the pressure lower than 2 bar and preferably in the temperature range of 400 DEG C to 700 DEG C, most preferably at the range of operation gas modifying catalyst 62 of 500 DEG C to 600 DEG C.9th volatile component can be recycled to following at least one: a) one or more treatment bench 50, b) dehydration catalyst 60, c) aromatized catalyst 61, d) gas modifying catalyst 62, and e) fuel gas treatment facility.

Although usually this technique is described as the production of recyclable fuel, but it also may be desirable for producing specific fuel, such as jet fuel, diesel oil, gasoline and kerosene or can easily by fusion to prepare the component of jet fuel, diesel oil, gasoline and kerosene.Jet and diesel fuel is the mixture of the different hydrocarbon in a large number with different carbon numbers (carbon atom of per molecule).Kerosene type jet fuel has between the carbon number distribution about between 8 and 16, and long distillate (wide-cut) or naphtha type jet fuel have between the carbon number distribution about between 5 and 15.Jet fuel has the aliphatic hydrocarbon higher than gasoline and lower arene content usually.Diesel oil gas, than jet fuel weight, has more slightly large hydrocarbon chain, but both all mainly paraffin oil (kerosene).

Fig. 4 is the embodiment for the production for renewable jet fuel, diesel oil, gasoline and kerosene component.In this embodiment, the series of selective catalysis reactor is to comprise oxygenatedchemicals synthetic catalyst, dehydration catalyst, alkene production catalyst and olefin oligomerization catalyst.System 400 is made up of N number of shown in Fig. 4.First the living beings with unspecified composition experience the temperature T in treatment bench 1 _{start 1}.T _{start 1}selected by operator.It is selected based on the composition of living beings, or to reach the Optimal Production of volatile component.T _{start 1}usually can in the scope of 200 DEG C to 500 DEG C, and be preferably from 300 DEG C to 550 DEG C in some cases.To living beings with apply compression shock deposit in case by apply heat can obtain this temperature.The amplitude of compression shock preferably changes to 10GPa from 0.2MPa in some embodiments, and most preferably from 0.5MPa to 5GPa.The heating of the living beings in platform 1 and/or pressure produce the first escaping gas and non-volatile carbon solid, are labeled as the solid 1 in Fig. 4.The first product of the second volatile component, the first recyclable fuel and water is produced when escaping gas experience catalytic dehydration post 161 is to produce cooling.Then, the second volatile component experience catalyst for oligomerization 162 primarily of C2-C5 alkene composition is cooled to 0-20 DEG C to produce, and exports the 3rd volatile products when being preferably cooled to 0-5 DEG C in some cases and comprise second product of the second recyclable fuel of mixture of gasoline and diesel oil distillate.According to one or more embodiment, the feature of the renewable diesel fuel obtained from this technique is to make the diesel component of this second recyclable fuel experience hydrotreating catalyst 163 by cooling generation the 4th volatile component, renewable kerosene or renewable jet fuel and water in the presence of the hydrogen.The feature of the renewable jet fuel obtained from this technique according to one or more embodiment is

The solid 1 reclaimed from the technique of the first treatment bench in Fig. 4 then carries out the second gentleness progressively pyrolysis of living beings at treatment bench 2.This temperature can identical with the temperature in treatment bench 1 or its can be temperature T _{start 1}+ Δ Τ ₁, wherein, Δ Τ ₁the temperature increment selected by operator, and typically in the scope of 10-200 DEG C, preferred in the scope of 10-100 DEG C in some cases, and in some cases most preferably in the scope of 10-50 DEG C.Selective temperature increment thus realize living beings gentleness progressively pyrolysis become volatile component and described component changes into renewable jet fuel.To living beings with apply compression shock deposit in case by apply thermograde can realize temperature increment.In some embodiments, thermograde preferably can be changed to about 1000 DEG C/sec from about 0.001 DEG C/sec to T, and is most preferably changed to 100 DEG C/sec from about 0.01 DEG C/sec.In some embodiments, the amplitude of compression shock preferably can be changed to 10GPa from 0.2MPa, and is most preferably changed to 5GPa from 0.5MPa.The volatile component that the process at treatment bench 2 place is produced carry out forming with the above volatility produced about treatment bench 1 cited by identical a series of catalyst.Fig. 4 is that treatment bench 1 to N-1 illustrates the conversion of living beings to jet fuel, and at treatment bench N-1 place, carbon solid N-1 retains.

As shown in Figure 5, N number for the treatment of bench makes carbon solid N-1 experience temperature T _{start 1}+ Δ Τ _Ν, T _{start 1}+ Δ Τ _Νenough high to produce few volatile component and major part is remaining coke.This coke can be shifted subsequently to the extraneous gas converter unit that can comprise any conventional gasifier.Processing temperature and gasification temperature are greater than 700 DEG C usually.In some cases, gas converter unit makes the one in carbon solid N-1 and external water source, carbon dioxide, methane or fuel gas react.In other cases, this gas converter unit makes carbon solid N-1 react with the one in the inner carbon dioxide, water/carbinol mixture or the fuel gas that produce.The product of gas converter is synthesis gas (synthesis gas), its compressed and the catalysis post sent into containing oxidative synthesis catalyst 160 (such as dimethyl ether or methyl alcohol) to produce (2N-1) individual product.Make this product by water base separator with produce comprise water/methanol fraction recyclable fuel, along with carbon dioxide unreacted synthesis gas and mainly comprise the volatile component (4N-4) of dimethyl ether of the methyl alcohol with aequum.Water/methanol fraction and the unreacted synthesis gas with carbon dioxide can be discharged, be again transmitted back to gasifier, or for other objects, such as, run generating set.

Oxidative synthesis catalyst can the synthesis of catalysis oxygenatedchemicals, as aldehyde, alcohol, ketone, ether and carboxylate.This catalyst is known and can comprises the co-precipitation oxide of Cu and Zn.These oxides can with various oxide co-precipitation well known by persons skilled in the art to promote the formation equilibrating to dimethyl ether.Oxide comprises the oxide of aluminium, chromium, manganese, zirconium and boron.The typical ratios of Cu/Zn can be changed to 1:5 from 5:1.When aluminium oxide, Al/Cu ratio can be changed to 2 and Al/Zn ratio can be changed to 1 from 0.1 from 0.05.Typical catalyst operating temperature is 200 DEG C to 300 DEG C, and typical final compressor pressure is in the scope that 40 bar to 80 cling to, but pressure is low to moderate 10 bar may produce the conversion ratio close with the balance of some catalytic preparation.

With reference to figure 5, the volatile fraction 4N-4 be made up of oxygenate (oxygenates) can be fed to dehydration catalyst 161, and it produces 2N product.When at cold-trap cooling (in some cases, preferably in the scope of 0-5 DEG C) of 0-20 DEG C, this produces 2N recyclable fuel and by C ₂-C ₅the volatile component that alkene (4N-3) forms.Dehydration catalyst 161 can comprise any known acid catalyst such as SAPO-34, the ZSM-5 type catalyst of such as ZSM-5, A1PO ₄zSM-5, ZSM-11 and MCM-22 of modification.These catalyst are used for methyl alcohol/DME to alkene (MTO) technique.Typical operating temperature is 300 DEG C-600 DEG C, and typical operating pressure is 0.1-10 bar.The alkene produced can comprise C ₂, C ₃, C ₄and C ₅the mixture of alkene, comprises structure and the stereoisomer of ethene, propylene, butylene, amylene and these alkene.

These alkene to produce (2N+1) individual product, can produce primarily of C when it cools in cold-trap in catalyst for oligomerization 162 in oligomerisation ₆-C ₂₀(2N+1) individual recyclable fuel component that alkene (in gasoline and diesel range) forms and volatile component (4N-2).Catalyst for oligomerization 162 can comprise the acid catalyst being similar to the foregoing MTO stage, but operating condition is different, and pressure is in the scope of 10-60 bar, and temperature is in the scope of 200 DEG C to 350 DEG C.Volatile component (4N-2) can be transmitted back to gasifier.

The diesel component of (2N+1) the individual liquid recyclable fuel that oligomerisation process can be produced is transported in the reactor comprising hydrotreating catalyst 163 together with hydrogen, produce the product producing renewable jet fuel, diesel fuel, kerosene component and volatile component (4N+1) when being cooled to 0-20 DEG C (in some cases, being preferably cooled to 0-5 DEG C).Volatile component (4N+1) can recycle gets back to gasifier.Hydrotreatment or hydrogenation processing catalyst comprise CoMo, NiMO, high pore volume Ni and high pore volume Mo.The recyclable fuel of gained can comprise the mixture of the liquid fuel usually classifying as kerosene, diesel fuel, jet fuel or aviation gasoline.

Above-mentioned embodiment 3 relates to the understanding utilized the initial composition of living beings charging, then based on the method for the route of this initial composition adjustment catabolite.Therefore, consider the raw material being rich in hemicellulose, it is beneficial that all treatment benches 50 may be set to that temperature is greater than 300 DEG C.Similarly, consider the raw material being rich in lignin, it is beneficial that may operate all treatment benches 50 being greater than at the temperature of 500 DEG C.Expect that this operation utilizes all platforms in the most efficient manner to maximize fuel output.

Another kind method needs to use a kind of algorithm, and this algorithm improves independent treatment bench temperature Δ Τ until reach required final temperature.The method is shown in Figure 6, and it shows the temperature algorithm flow chart 600 of single treatment bench.For three shuntings (cut) derived from lipid, hemicellulose and lignin, T can be selected _lowfor about 300 DEG C, and T _highfor about 500 DEG C.

With reference to Fig. 6, in operation 405, T=T _start.Operation 410 relates to raising living beings temperature Δ Τ.Then, operate 415 to relate to and determining for lipid whether T<T _low.If like this, following step needs conveying living beings by lipid catalyst chain (operation 420), collects product (operation 425) and continue living beings temperature to be improved Δ Τ (operation 410).If operation 415 is negatives, operation 440 relates to be determined for hemicellulose whether T _low<T<T _high.if like this, following step comprises conveying living beings by hemicellulose catalyst chain (operation 445), collects product (operation 450), and continues living beings temperature to be improved Δ Τ (operation 410).If operation 440 is negatives, operation 470 relates to be determined for lignin whether T>T _high.If like this, following step needs conveying living beings by catalytic lignin agent chain (operation 475), collects product (operation 480), and proceeds to living beings temperature rising Δ Τ (operation 410).If operation 470 is negatives, algorithm terminates.

Another kind of method is also had to relate to the output of load balancing from each catalysis chain to improve the output of product to greatest extent.This method is shown in Figure 7, which depict the load balancing algorithm flow chart 700 for a treatment bench.According to the method, do not need to understand composition.On the contrary, export output by the product of more each route and determine optimum catalysis route.As a result, increasing temperature is until realize final preferred temperature.

With reference to Fig. 7, at operation 505 place T=T _start.Operation 510 relates to opens all routes.Then, operate 515 to comprise and make living beings temperature improve Δ Τ.At this point, the method is divided into three routes, particularly catalyst chain A (operation 520), catalyst chain B (operation 525) and catalyst chain C (operation 530).In operation 540,545,550 subsequently, product is collected to each catalyst chain.Operation 560 needs to determine best catalysis route, is exported output by the product compared from each route and is determined to have the catalyst chain calculating of the highest Product yields.Then, operation 565 comprises all routes of closedown, except having the route of maximum output.Operation 570 relate to determine whether product export lower than threshold value.If like this, then algorithm continues to open all routes (operation 510).If not, algorithm continues living beings temperature to be raised Δ Τ (operation 515).

exemplary embodiment 1

Referring now to Fig. 8 A, this exemplary embodiment is equivalent to 6 treatment benches 50 run at six different temperature, wherein inputs living beings charging and remove final carbon solid at 575 DEG C at 325 DEG C.Living beings (it is the living beings the being rich in lipid) devolatilization together with the dimethyl ether as cosolvent that 150g is made up of business sunflower seeds, starts and terminates at 575 DEG C, temperature increment per hour 50 DEG C at the temperature of 325 DEG C.Make the methyl alcohol of 131g by silica gel aluminium oxide catalyst to produce required cosolvent.As shown in Figure 3, for shunting A, make output by comprising the different catalysis post of three of series connection of dehydration catalyst 60, aromatized catalyst 61 gentle body modifying catalyst 62.More specifically, this experiment uses silica-alumina dehydration catalyst, the ZSM-5 aromatized catalyst of Zn and Cr modification and the ZSM-5 gas modifying catalyst of Ga modification.Fig. 8 A is the chart being presented at the fuel collected in the halfhour time interval often kind of catalyst at each temperature.During end of run, three kinds of catalyst produce the recyclable fuel amounting to 46.5ml, comprise: the recyclable fuel of the total 26.5ml that (i) collects from aromatized catalyst 61, (ii) from the recyclable fuel of total 18ml that dehydration catalyst 60 is collected, and the recyclable fuel of total 2ml that (iii) collects from gas modifying catalyst 62.

Fig. 8 B is the gas-chromatography map contour of the recyclable fuel that display is collected from dehydration catalyst 60 and the chart of the comparison chart of conventional U.S. diesel oil #2 and biodiesel B99 that obtains from commercial source.The recyclable fuel produced from dehydration catalyst according to the present invention is remarkable compared to biodiesel B99 different and be more similar to the profile of conventional U.S. diesel oil #2.The gas chromatograph figure shown in Fig. 8 C and 8D represents the recyclable fuel composition from the gentle body modifying catalyst 62 of aromatized catalyst 61 respectively.The aromatic hydrocarbons of significant quantity is present in these two kinds of recyclable fuels.

exemplary embodiment 2

This exemplary embodiment is equivalent to 6 treatment benches run at six different temperature, wherein inputs living beings charging and remove final carbon solid at 525 DEG C at 325 DEG C again.The living beings that 76g is made up of commercial corn cob, together with 100g methyl alcohol devolatilization, start and terminate at the temperature of 525 DEG C, temperature increment per hour 50 DEG C at the temperature of 325 DEG C.The present embodiment hypothesis corncob contains the hemicellulose (C5 sugar) of significant quantity, and it can decompose under the existence of dehydration catalyst 60, thus causes than required more chemical bond rupture.Therefore, for shunting B, as shown in Figure 3, make output by two different catalysis posts of series connection, one is made up of aromatized catalyst 61, is then gas modifying catalyst 62.In the present embodiment, ZSM-5 is used as aromatized catalyst, and the ZSM-5 of Ga modification is used as gas modifying catalyst.Collect the recyclable fuel of 29ml altogether during end of run from aromatized catalyst, and collect the recyclable fuel of 5.5ml altogether from gas modifying catalyst.There is aromatic compounds similar shown in the upper and exemplary embodiment of composition in the further analytical table of these the two kinds of recyclable fuels collected obviously work.

exemplary embodiment 3

This exemplary embodiment is equivalent to 6 treatment benches run at six different temperature, wherein inputs living beings charging and remove final carbon solid at 525 DEG C at 325 DEG C again.The living beings that 100g is made up of red fir wood, together with 131g methyl alcohol devolatilization, start and terminate at the temperature of 525 DEG C, temperature increment per hour 50 DEG C at the temperature of 325 DEG C.The present embodiment hypothesis red fir contains the lignin of significant quantity, and it needs to be decomposed so that effective biomass conversion.Make output by two different catalysis posts of series connection, starting from dehydration catalyst 60, is then aromatized catalyst 61.The present embodiment utilizes silica alumina as dehydration catalyst, and the ZSM-5 of Zn and Cr modification is as aromatized catalyst.Collect the recyclable fuel of 30.5ml altogether during end of run from aromatized catalyst 61, and collect the recyclable fuel of 1ml altogether from dehydration catalyst 60.Although the fuel-based coming from silica alumina catalyst is similar to diesel oil, the fuel from aromatized catalyst contains the aromatic hydrocarbons of significant quantity.Escaping gas after aromatized catalyst 61 has the C of significant quantity ₁-C ₅noncondensable hydrocarbon, as shown in Figure 9.

exemplary embodiment 4

This exemplary embodiment to be equivalent at six different temperature (alternatively, this temperature can keep constant at each treatment bench) 6 treatment benches operating, wherein, living beings charging and remove final carbon solid at 525 DEG C at 325 DEG C is again inputted.Living beings together with methyl alcohol start devolatilization and terminate at 575 DEG C at the temperature of 325 DEG C, and temperature increment hourly is 50 DEG C.Make output by the different catalysis posts of three kinds of series connection, starting from dehydration catalyst, is then catalyst for oligomerization, and is finally hydrotreating catalyst.Reproducible jet fuel is collected from hydrotreating catalyst during end of run.Jet fuel from hydrotreating catalyst is rich in aliphatic hydrocarbon and is applicable to mix with other component to prepare renewable jet fuel.

According to various exemplary and implementation, the present invention is described although above, should be understood that, in describing in one or more independent embodiment and the applicability of function be not limited to describe their specific embodiments, but can apply separately or be applicable to one or more other embodiments of the present invention with various combination, the part no matter whether these embodiments are described as and no matter whether these features show as described embodiment.Therefore, each or each embodiment described above can combine with any one or other embodiments multiple.Therefore, range of the present invention and scope should not be subject to the restriction of any above-mentioned exemplary.

Unless expressly stated otherwise, the term used in this document and phrase and variant thereof should be interpreted as open instead of restrictive.Example as above-mentioned: term " comprises " and should be understood to imply " including but not limited to " etc.; Term " embodiment " is for providing the illustrative examples of discussed project, instead of its exhaustive and restrictively to enumerate; Term " one (a) " or " one (a) " should be understood to imply " at least one ", " one or more " etc.; And adjective such as " routine ", " traditional ", " normally ", " standard ", the term of " known " and similar meaning should not be interpreted as described project to be restricted to given period or preset time available project, but should be understood to include now or in technology that the is routine that can obtain or know any time in the future, traditional, normal or standard.Similarly, when this document quotes or known technology obvious for those of ordinary skill in the art, this technology comprises the obvious or known technology now or in any time in future for those skilled in the art.

In some example, widen word and phrase such as " one or more ", " at least ", the existence of " but being not limited to " or other similar phrases should not be understood to represent and intends or need narrower situation may not there is this widening in the example of phrase.In addition, according to block diagram, flow chart and other diagrams, the various embodiments enumerated are described herein.It is evident that after those skilled in the art read this document, the embodiment illustrated and various alternative thereof can be implemented when being not limited to the embodiment illustrated.These illustrations and its adjoint description should not be interpreted as mandatory requirement certain architectures or configuration.

Claims (85)

1., for biomass conversion being become a system for diesel oil or jet fuel, it comprises:

Comprise the device of multiple treatment bench (N) and a series of catalyst;

Each treatment bench can make the living beings in described experience at least one initial temperature (T _start) to produce volatile component and nonvolatile element;

For being received at least one catalytic reactor of the volatile ingredient produced in each treatment bench; With

Wherein, at least one catalytic reactor described comprises the catalyst being selected from dehydration catalyst, olefin oligomerization catalyst and hydrotreating catalyst.

2. system according to claim 1, also comprises extra catalytic reactor.

3. system according to claim 2, wherein, series connection uses described extra catalytic reactor.

4. system according to claim 2, wherein, the described extra catalytic reactor of use in parallel.

5. system according to claim 1, also comprises the temperature controller for being increased progressively independent treatment bench temperature by increment (Δ T).

6. system according to claim 1, wherein, described nonvolatile element is carbonaceous material.

7. system according to claim 1, also comprises the gasifier for converting carbonaceous material being become synthesis gas.

8. system according to claim 7, also comprises the conduit for introducing synthesis gas from described gasifier to catalytic reactor.

9. system according to claim 1, wherein, N is in the scope of 2 to 1000, and wherein T _startin the scope of 100 DEG C to 1000 DEG C.

10. system according to claim 5, wherein, described temperature increment (Δ T) is in the scope of 0 DEG C to 200 DEG C.

11. systems according to claim 1, also comprise for holding co-fed reservoir, with for by the described co-fed conduit be incorporated in described volatile component or treatment bench described at least one, wherein, describedly co-fedly alcohols, aldehydes, ketone, ethers, carboxylic acids and hydro carbons is selected from.

12. systems according to claim 11, also comprise the conduit from gasifier to the catalytic reactor containing syngas conversion catalyst, wherein, describedly co-fedly to be produced by described syngas conversion catalyst.

13. systems according to claim 1, described living beings are selected from lipid, hemicellulose, cellulose and lignin.

14. systems according to claim 13, wherein, described living beings are the mixtures being selected from lipid, hemicellulose, cellulose and lignin two kinds or more kinds of living beings.

15. systems according to claim 13, wherein, have the type selecting T of the living beings of maximum concentration in the mixture according to described two kinds or more kinds of living beings _start.

At least 2 treatment benches wherein, are set as identical T by 16. systems according to claim 1 _start.

17. systems according to claim 1, wherein, are set as identical T by all treatment benches _{open begin}.

18. systems according to claim 1, wherein, T _startit is the temperature of substantial constant.

19. systems according to claim 1, wherein, described nonvolatile element is heat conduction.

20. systems according to claim 1, wherein, the described nonvolatile element at N number for the treatment of bench place comprises coke.

21. systems according to claim 1, wherein, N number for the treatment of bench comprises the input of fuel gas that can accept recirculated water that external water source, carbon dioxide or methane or inside provides or be caused by catalyst treatment.

22. systems according to claim 1, wherein, described dehydration catalyst comprises the combination of any acid catalyst or acid catalyst.

23. systems according to claim 1, wherein, described olefin oligomerization catalyst is dehydration catalyst.

24. systems according to claim 1, also comprise conduit with the water will produced in described system, carbon dioxide and methyl alcohol guiding gasifier, for the conversion of described nonvolatile element to synthesis gas.

25. systems according to claim 24, wherein, the described nonvolatile element from platform comprises the raw material for next platform.

26. systems according to claim 1, wherein, the diesel oil of generation or jet fuel comprise one or more kerosene component.

27. systems according to claim 1, wherein, the diesel oil of generation or jet fuel comprise one or more jet fuel components.

28. systems according to claim 1, wherein, the diesel oil of generation or jet fuel comprise one or more diesel fuel constituents.

29. systems according to claim 6, wherein, the water of inner generation, carbon dioxide, methyl alcohol are used as described carbonaceous material to the reactant in the conversion of synthesis gas.

30. systems according to claim 1, wherein, described treatment bench is selected from pyrolysis reactor, fixed bed reactors, fluidized-bed reactor, circulating bed reactor, bubbling fluidization bed bioreactor, vacuum moving-burden bed reactor, drainage type reactor, cyclonic reactor, vortex reactor, rotating cone reactor, helical reactors, ablation reactor, the pyrolysis reactor of microwave radiation technology, the pyrolysis reactor of plasmaassisted, the chamber in living beings fractionating system, gasifier and vacuum moving-burden bed reactor.

31. 1 kinds for coke being become the system of recyclable fuel, it comprises: the device comprising multiple treatment bench (N) and a series of catalyst; Each treatment bench can make the coke in described experience at least one initial temperature (T _start) to produce synthesis gas; For being received at least one catalytic reactor of the synthesis gas produced in each treatment bench; Wherein, at least one catalytic reactor described comprises the catalyst being selected from syngas conversion catalyst, methanol synthesis catalyst, DME synthetic catalyst, dehydration catalyst, olefin oligomerization catalyst and hydrotreating catalyst.

32. systems according to claim 31, also comprise extra catalytic reactor.

33. systems according to claim 32, wherein, series connection uses described extra catalytic reactor.

34. systems according to claim 32, wherein, the described extra catalytic reactor of use in parallel.

35. systems according to claim 31, wherein, described treatment bench is selected from pyrolysis reactor, fixed bed reactors, fluidized-bed reactor, circulating bed reactor, bubbling fluidization bed bioreactor, vacuum moving-burden bed reactor, drainage type reactor, cyclonic reactor, vortex reactor, rotating cone reactor, helical reactors, ablation reactor, the pyrolysis reactor of microwave radiation technology, the pyrolysis reactor of plasmaassisted, the chamber in living beings fractionating system, gasifier and vacuum moving-burden bed reactor.

36. systems according to claim 31, also comprise the temperature controller for being increased progressively independent treatment bench temperature by increment (Δ T).

37. systems according to claim 31, wherein, N is in the scope of 2 to 1000, and wherein T _startin the scope of 100 DEG C to 1000 DEG C.

38. systems according to claim 36, wherein, described temperature increment (Δ T) is in the scope of 0 DEG C to 200 DEG C.

39. systems according to claim 31, also comprise for holding co-fed reservoir, with for by the described co-fed conduit be incorporated in described volatile component or treatment bench described at least one, wherein, describedly co-fedly alcohols, aldehydes, ketone, ethers, carboxylic acids and hydro carbons is selected from.

40. systems according to claim 31, wherein, N number for the treatment of bench comprises the input of fuel gas that can accept recirculated water that external water source, carbon dioxide or methane or inside provides or be caused by catalyst treatment.

41. systems according to claim 31, wherein, described dehydration catalyst comprises the combination of any acid catalyst or acid catalyst.

42. systems according to claim 31, wherein, described olefin oligomerization catalyst is dehydration catalyst.

43. systems according to claim 31, wherein, described recyclable fuel comprises one or more kerosene component, or one or more jet fuel components.

44. 1 kinds of methods for by biomass conversion being diesel oil or jet fuel, it comprises:

Living beings are assigned in multiple treatment bench (N);

The living beings in described are made to experience at least one initial temperature (T _start) to produce volatile component and nonvolatile element;

Described volatile component is imported at least one catalytic reactor, and described at least one catalytic reactor designs becomes to implement to be selected from one or more techniques of dehydration, olefin(e) oligomerization and hydrotreatment;

Be collected in the diesel oil or jet fuel that produce at least one catalytic reactor described.

45. methods according to claim 44, also comprise extra catalytic reactor.

46. methods according to claim 45, wherein, series connection uses described extra catalytic reactor.

47. methods according to claim 45, wherein, the described extra catalytic reactor of use in parallel.

48. methods according to claim 44, also comprise and utilize temperature controller to increase progressively independent treatment bench temperature by increment (Δ T).

49. methods according to claim 44, wherein, described nonvolatile element is carbonaceous material.

50. methods according to claim 44, also comprise and converting carbonaceous material are become synthesis gas.

51. methods according to claim 44, wherein, N is in the scope of 2 to 1000, and wherein T _startin the scope of 100 DEG C to 1000 DEG C.

52. methods according to claim 44, wherein, described temperature increment (Δ T) is in the scope of 0 DEG C to 200 DEG C.

53. methods according to claim 1, also comprise and are incorporated into described volatile component or treatment bench described at least one by co-fed, wherein, are describedly co-fedly selected from alcohols, aldehydes, ketone, ethers, carboxylic acids and hydro carbons.

54. methods according to claim 53, also comprise the catalytic reactor comprising syngas conversion catalyst, wherein, describedly co-fedly to be produced by described syngas conversion catalyst.

55. methods according to claim 44, wherein, described living beings are selected from lipid, hemicellulose, cellulose and lignin.

56. methods according to claim 55, wherein, described living beings are the mixtures being selected from lipid, hemicellulose, cellulose and lignin two kinds or more kinds of living beings.

57. methods according to claim 56, wherein, have the type selecting T of the living beings of maximum concentration in the mixture according to described two kinds or more kinds of living beings _start.

At least 2 treatment benches wherein, are set as identical T by 58. methods according to claim 44 _start.

59. methods according to claim 44, wherein, are set as identical T by all treatment benches _start.

60. methods according to claim 44, wherein, T _startit is the temperature of substantial constant.

61. methods according to claim 44, wherein, described nonvolatile element is heat conduction.

62. methods according to claim 44, wherein, the described nonvolatile element at N number for the treatment of bench place comprises coke.

63. methods according to claim 44, wherein, N number for the treatment of bench comprises the input of fuel gas that can accept recirculated water that external water source, carbon dioxide or methane or inside provides or be caused by catalyst treatment.

64. methods according to claim 44, wherein, described dehydration catalyst comprises the combination of any acid catalyst or acid catalyst.

65. methods according to claim 44, wherein, described olefin oligomerization catalyst is dehydration catalyst.

66. methods according to claim 44, wherein, the water produced in described system, carbon dioxide and methyl alcohol are for the conversion of described nonvolatile element to synthesis gas.

67. methods according to claim 44, wherein, the described nonvolatile element from platform comprises the raw material for next platform.

68. methods according to claim 44, wherein, the diesel oil of generation or jet fuel comprise one or more kerosene component.

69. methods according to claim 44, wherein, the diesel oil of generation or jet fuel comprise one or more jet fuel components.

70. methods according to claim 44, wherein, the diesel oil of generation or jet fuel comprise one or more diesel fuel constituents.

71. methods according to claim 49, wherein, the water of inner generation, carbon dioxide, methyl alcohol are used as described carbonaceous material to the reactant in the conversion of synthesis gas.

72. methods according to claim 44, wherein, described treatment bench is selected from pyrolysis reactor, fixed bed reactors, fluidized-bed reactor, circulating bed reactor, bubbling fluidization bed bioreactor, vacuum moving-burden bed reactor, drainage type reactor, cyclonic reactor, vortex reactor, rotating cone reactor, helical reactors, ablation reactor, the pyrolysis reactor of microwave radiation technology, the pyrolysis reactor of plasmaassisted, the chamber in living beings fractionating system, gasifier and vacuum moving-burden bed reactor.

73. 1 kinds for coke being become the method for diesel oil or jet fuel, it comprises:

Coke is assigned to multiple treatment bench (N);

Make the coke in described experience at least one and start temperature (T _start) to produce synthesis gas;

Described synthesis gas is imported at least one catalytic reactor, and described at least one catalytic reactor designs becomes to implement to be selected from Synthetic holography catalysis, methanol synthesis catalyst, DME synthesis catalytic, dehydration, olefin(e) oligomerization gather and one or more techniques of hydrotreatment;

Be collected in the diesel oil or jet fuel that produce at least one catalytic reactor described.

74. according to the method described in claim 73, also comprises extra catalytic reactor.

75. according to the method described in claim 74, and wherein, series connection uses described extra catalytic reactor.

76. according to the method described in claim 74, wherein, and the described extra catalytic reactor of use in parallel.

77. according to the method described in claim 73, and wherein, treatment bench is selected from by pyrolysis reactor, fixed bed reactors, fluidized-bed reactor, circulating bed reactor, bubbling fluidization bed bioreactor, vacuum moving-burden bed reactor, drainage type reactor, cyclonic reactor, vortex reactor, rotating cone reactor, helical reactors, ablation reactor, the pyrolysis reactor of microwave radiation technology, the pyrolysis reactor of plasmaassisted, the chamber in living beings fractionating system, gasifier and vacuum moving-burden bed reactor.

78. according to the method described in claim 73, also comprises and utilizes temperature controller to increase progressively independent treatment bench temperature by increment (Δ T).

79. according to the method described in claim 73, and wherein, N is in the scope of 2 to 1000, and wherein T _startin the scope of 100 DEG C to 1000 DEG C.

80. according to the method described in claim 78, and wherein, described temperature increment (Δ T) is in the scope of 0 DEG C to 200 DEG C.

81. according to the method described in claim 73, also comprises and is incorporated into described volatile component or treatment bench described at least one by co-fed, wherein, is describedly co-fedly selected from alcohols, aldehydes, ketone, ethers, carboxylic acids and hydro carbons.

82. according to the method described in claim 73, and wherein the N number for the treatment of bench receives the recirculated water that external water source, carbon dioxide or methane or inside provide or the fuel gas caused by catalyst treatment.

83. according to the method described in claim 73, and wherein, described dehydration catalyst comprises the combination of any acid catalyst or acid catalyst.

84. according to the method described in claim 73, and wherein, described olefin oligomerization catalyst is dehydration catalyst.

85. according to the method described in claim 73, and wherein, described recyclable fuel comprises one or more kerosene component or one or more jet fuel components.