CN105377416A

CN105377416A - Steam explosion methods before gasification

Info

Publication number: CN105377416A
Application number: CN201480027130.2A
Authority: CN
Inventors: F·M·费拉罗; J·W·霍曼; R·S·安皮斯基
Original assignee: Sundrop Fuels Inc
Current assignee: Sundrop Fuels Inc
Priority date: 2013-05-14
Filing date: 2014-05-14
Publication date: 2016-03-02
Also published as: WO2014204519A1; JP2016526065A

Abstract

An integrated plant that includes a steam explosion process unit and biomass gasifier to generate syngas from biomass is discussed. A steam explosion process unit applies a combination of heat, pressure, and moisture to the biomass to make the biomass into a moist fine particle form. The steam explosion process unit applies steam with a high pressure to heat and pressurize any gases and fluids present inside the biomass to internally blow apart the bulk structure of the biomass via a rapid depressurization of the biomass with the increased moisture content. Those produced moist fine particles of biomass are subsequently fed to a feed section of the biomass gasifier, which reacts the biomass particles in a rapid biomass gasification reaction to produce syngas components.

Description

Steam explosion method before gasification

related application

This international application advocates that the title submitted on May 13rd, 2014 is the U. S. application the 14/276th of " pretreatment (PretreatmentofBiomassUsingSteamExplosionMethodsBeforeGas ification) using the living beings of the steam explosion method before gasification ", the priority of No. 719 and rights and interests, described U. S. application advocates that the title submitted to as on June 22nd, 2012 is U.S.'s non-provisional application the 13/531st of " pretreatment (PretreatmentofBiomassUsingSteamExplosionMethodsBeforeGas ification) using the living beings of the steam explosion method before gasification ", No. 318 part continuity priority and rights and interests.According to 35U.S.C. § 119, the application also advocates that the title submitted on May 14th, 2013 is priority and the rights and interests of No. the 61/823rd, 360, the U.S. Provisional Application of " pretreatment (PretreatmentofBiomassUsingSteamExplosionMethodsBeforeGas ification) using the living beings of the steam explosion method before gasification ".The application also advocates that the title submitted to as on June 4th, 2013 is priority and the rights and interests of the part continuity of No. PCT/US2013/044143rd, the PCT application of " pretreatment (PretreatmentofBiomassUsingSteamExplosionMethodsBeforeGas ification) using the living beings of the steam explosion method before gasification ", described PCT application advocates above-mentioned U.S. Provisional Application the 61/823rd, No. 360 and U.S.'s non-provisional application the 13/531st, the priority of No. 318 and the international application of rights and interests; All above-mentioned applications are incorporated to by reference at this.

Technical field

The design relates generally to the process using steam explosion method as the pretreated living beings before gasification or burning.In an embodiment, the design relates in particular to a kind of integrated equipment, it uses these living beings to produce liquid fuel from described living beings, or described living beings is converted to densified form to promote to be transferred to facility economically for being further processed as liquid fuel, heat/electric power, animal feed, bedding or chemicals.

Background technology

The technology of initial conception is the fiberboard making intermediate density of dry wood chip.Other process entails grinding wood chip, make that chip is dry, the multiple steps cutting bits, make fiber moisturizing, make fiber densification, then make wood chip densified (being such as the form of particle) of regrinding.These processes are complicated, need use substantial contribution and need mass energy.Some other canonical process needs to make living beings chip dry, then chip is ground to very small dimensions and they is sent to follow-up heating/processing unit subsequently.This drying and grinding spend a large amount of energy and fund cost.These processes produce the manyfold that fubril but its size are the fine grain sizes produced by steam blasting process (SEP).The Previous industrial of SEP process is used to wish to maintain integrality and the fibre strength of the fiber forming living beings; And therefore there is the longer fragment do not stood as the harsh conditions in steam blasting unit.Equally, the additional machinery of non-applying biological matter stirs, because this will reduce fibre length and integrality further.

Summary of the invention

A kind of integrated equipment, it comprises steam blasting unit and biomass gasifying furnace to produce synthesis gas from living beings.The fine particulate form that the Combination application of heat, pressure and moisture is become moist to living beings to make living beings by steam blasting unit.The steam that steam blasting unit application has high pressure heats with any gas existed living beings inside and fluid and pressurizes.Wherein at the outlet opening place to two sections or more sections, through the overall structure of Pressed bio matter in inside by divide with via have raising moisture living beings reduction of blood pressure in high-speed and at internal division.The fine grained of the humidity of those living beings produced is fed to the feeding district of biomass gasifying furnace subsequently, and it reacts to produce synthesis gas components with quick bio matter gasification reaction and biological particles.The steam blasting section of steam blasting unit is coupled to refining section, and refining section has one or more blade, and it is configured to leave steam blasting section in living beings by aperture and mechanically stirred living beings before purge pipeline.

Accompanying drawing explanation

Multiple graphic example embodiment relating to the design.

Figure 1A and 1B shows the flow schematic diagram of the embodiment of steam blasting unit, described steam blasting unit have to receive living beings be used as the input cavity of raw material, two or more steam supply input and in order to preprocessing biomass for follow-up two sections that are fed to biomass gasifying furnace or more sections.

Fig. 2 shows in order to produce synthesis gas and produce the embodiment of the flow chart of the integrated equipment of liquid fuel goods from living beings from synthesis gas.

Fig. 3-1 to 3-4 shows the alternative arrangements for Exempla bibiomass gasification furnace.

Fig. 4 A to Fig. 4 C show have by lignin around and the difference amplification level of the example living beings chip of the fibre bundle of the cellulose fibre be bonded together.

Fig. 4 D shows explosion and becomes the chip of living beings fine grain example living beings.

Fig. 4 E shows the living beings chip with mass of fibers that is that be worn or that be partly separated into individuals fibers.

Fig. 5 shows the flow schematic diagram of the embodiment of the radiant heat chemical reactor being configured to produce the chemicals comprising forming gas product.

Although the design can have various amendment and alternative form, show its specific embodiment by means of example in the drawings and will describe in detail in this article.The design should be understood to and is not limited to disclosed concrete form, but on the contrary, and intention contains all modifications of the spirit and scope belonging to the design, equivalent and replacement scheme.

Detailed description of the invention

In the following description, set forth many specific detail, such as the example of specified chemical goods, attached name component, connection, heat source etc., to provide the thorough understanding to the present invention's design.But, it will be apparent to those skilled in the art that and can put into practice the present invention's design when not having these specific detail.In other cases, not in detail but in block diagram, in fact describe the assembly or method known to avoid unnecessarily obscuring the present invention's design.Therefore, the specific detail set forth is only exemplary.Specific detail can be different from and still expect in the spirit and scope of the present invention's design.

In general, the pretreated Multi-instance process being used for living beings and the device be associated with the pretreatment of living beings are described.Graphic and text describes the various example implementations of the pretreated integrated equipment using living beings below.In an embodiment, integrated equipment contain at least steam blasting unit and biomass gasifying furnace to produce synthesis gas from living beings.Steam blasting unit can have to receive living beings be used as one or more input cavities of raw material, one or more steam supply input and in order to preprocessing biomass to make biological particles for follow-up two sections that are fed to biomass gasifying furnace or more sections.The fine particulate form that the combination that described section of use is applied to the heat of living beings, pressure and moisture becomes moist to make living beings.By application from the first steam supply input steam with start to be reduced in lignin and from the cellulose fibre of living beings hemicellulose between bonding and improve the moisture of the living beings received, steam blasting process decomposes the overall structure of the living beings received at least in part.In the end in one section, apply any gas that the steam from least atmospheric pressure 14 times of the second steam supply input exists living beings inside and fluid heats and pressurizes.Wherein at the outlet opening place from two sections or more sections, in the overall structure of internal division through Pressed bio matter.Via the overall structure of the reduction of blood pressure in high-speed division living beings of the close-burning living beings of the moisture and reduction with raising.The living beings being produced as moist fine particulate form from described section can have and are such as less than 70 micron thickness and the average-size being less than 500 microns long.The living beings fine grained of those humidities produced is fed to the feeding district of biomass gasifying furnace subsequently.Biomass gasifying furnace has reactor vessel, it is configured to the living beings of moist fine particulate form are reacted, and the living beings of the fine particulate form of described humidity have the surface area of increase and the granular size of reduction owing to the division by steam blasting unit compared to the living beings chip received in input cavity.Biomass gasifying furnace has the 3rd steam supply input and one or more heater, and depositing in the case of steam, react with quick bio matter gasification reaction in the holdup time of living beings in fine particulate form in reactor vessel between 0.1 second to 300.0 seconds thus produce at least synthesis gas components, comprising hydrogen (H2) and carbon monoxide (CO).

Possible biomass gasifying furnace embodiment has high-temperature steam supply input and one or more heater, such as gas burner or storage heater.Depositing in the case of steam, by reacting with quick bio matter gasification reaction thus form synthesis gas components at higher than the temperature of 700 degrees Celsius within the holdup time being less than one second in reactor vessel in biomass gasifying furnace of the biological particles of steam blasting unit decomposition, comprise hydrogen (H2) and carbon monoxide (CO), described synthesis gas components is fed to methyl alcohol (CH30H) synthesis reactor.Be understood by those skilled in the art that the design hereafter discussed in this illustrative document mass part and in can be used as independent concept or the use that is bonded to each other.

When not carrying out extra drying, the water content in the living beings in chip formation entered can be change in the scope of 15% to 60% of the living beings staying outside.Can by producing living beings chip with the wood chipping equipment unit 104 of some filter fits, described filter has and is less than about one inch and the size of the chip of about 0.5 inch of average length and 0.25 inch of average thickness on average in order to be formed.(see such as Fig. 4 a, it illustrates the living beings chip 451 from one piece of living beings 453) living beings wood chipping equipment unit 104 can hit containing in order to cut and cut the four or more blade of living beings.The protrusion distance of the feed speed of biomass briquette, the speed of blade, cutter and nose angle can all in order to control chip size.Then screen chip and again cut those excessive chips.Can fusion from the chip of not homology or timber kind to strengthen some attribute.Magnet or other scanner can be made to pass through to detect and removal of impurity.To bring into use, initial low pressure saturated vapor decomposes, hydration process/moistening and softening living beings chip to be fed to living beings chip to be placed in pressure vessel in thermal decomposition section in steam blasting unit 108 on a conveyor or possibly.Low-pressure saturated steam can under 100 degrees Celsius.System can also inject some glidants (such as, from the recirculation ashes of biomass gasifying furnace 114) to prevent from being blocked by living beings chip and blocking in this position.

Wood chipping equipment unit 104 can be fed to and steam blasting unit 108 is configured to receive the biomass material of two or more types, wherein dissimilar living beings comprise 1) cork, 2) hardwood, 3) grass, 4) plant shell and 5) any combination, its in steam blasting unit 108 through fusion and Steam explosion treatment for homogenizing through roasting raw material, be collected subsequently and be then fed to biomass gasifying furnace 114.Steam blasting unit 108, drier 112 and biomass gasifying furnace 114 are designed to feeding neatly, do not change the physical Design of feeding supply equipment or the physical Design of biomass gasifying furnace 114 via the granular size at least controlling to produce from the biological particles of steam blasting section and drier 112.Drier 112 can be flash dryer, rotary drum drier, pedal-type dryer, air dryer or similar such device.

As discussed, magnetic filter and air cleanness filter system can be coupled to hot water processing section to guarantee that the living beings in chip formation eliminated metal fragment and ratchel before entering hot water processing section.Magnetic filter and air cleanness filter system prevent any metal fragment and/or ratchel blocking from comprising the part of the steam blasting unit of discharging outlet.Air cleanness filter system help abandons in fact ratchel and lightweight sand.It should be noted that the aperture that the discharge forming steam blasting section exports can be such as 0.25 to 0.375 inch.

Steam blasting unit 108 have to receive living beings be used as the input cavity of raw material, one or more steam supply input and in order to preprocessing biomass for follow-up two sections that are fed to biomass gasifying furnace 114 or more sections.The fine particulate form that the combination that described section of use is applied to the heat of living beings, pressure and moisture becomes moist to make living beings.By application from low-pressure steam supply input steam with start to be reduced in lignin and from the cellulose fibre of living beings hemicellulose between bonding and improve the moisture of the living beings received, steam blasting process decomposes the overall structure of the living beings received at least in part.(see such as Fig. 4 B, its illustrate have by lignin around and the living beings chip of the fibre bundle of the cellulose fibre be bonded together) in the end in one section, apply any gas that the steam from least atmospheric pressure 14 times of high steam feed end exists living beings inside and fluid heats and pressurizes, to divide the overall structure of the living beings received via the reduction of blood pressure in high-speed of the close-burning living beings of the moisture and reduction with raising in inside.

In an embodiment, two sections of steam blasting unit 108 or more sections comprise at least hot water processing section and steam blasting section.

The input cavity that hot water processing section has the chip receiving living beings and the low-pressure steam supply input in being applied to low-pressure saturated steam containing living beings chip container.Hot water processing section is configured to receive the living beings in chip formation, comprises leaf, needle, stem skin and timber.Low-pressure steam is applied to living beings by hot water processing section at the temperature of the glass transition point higher than lignin, to soften and to improve the moisture of living beings, therefore in steam blasting section living beings cellulose fibre can simply from the living beings in chip formation at internal division.In an embodiment, use steam that living beings chip is heated to above 60 DEG C.Low-pressure saturated steam is applied under higher than 60 degrees Celsius but lower than the high temperature of 145 degrees Celsius in the container containing living beings chip by low-pressure steam supply input under the pressure of about normal pressure PSI, thus start to decompose, hydration process the softening living beings in chip formation received.Low pressure feed input can be made up of some nozzles that strategy is placed around container.The high temperature of one group of temperature sensor to the living beings chip received provides feedback.Control system is configured to the holdup time keeping living beings chip to stop in hot water processing section 8 to 20 minutes, and described holdup time long enough soaked into living beings chip with moisture before being moved out to steam blasting section in living beings.There is the shorter holdup time in the wooden unit for the trunk from tree, and there is the longer holdup time for branch, needle etc.

Hot water processing section may will be fed to steam blasting section through softening and that moisture improves living beings chip via screwfeed system.The pressure of steam blasting section is maintained 10 to 30 times of the pressure existed in hot water processing section and maintains at high temperature by control system, the temperature of such as 160 to 270 DEG C, preferably, and 190 DEG C to 220 DEG C.Pressure can under 180 to 450 pounds/square inch (PSI) (preferably, 300PSI).The moisture of living beings is elevated to by weight at least 40% by steam blasting section further, and preferably, the moisture of 50% to 60% by weight.Moisture percentage by weight can be that the weight of water adds divided by by living beings chip the gross weight that water weight is formed.In steam blasting section, warp is softening and moisture living beings chip is exposed to the sufficient time section continuing 3 minutes to 15 minutes in high temperature and high pressure steam, forms high steam with other inside, porous zone in the overall structure of the cellulose fiber peacekeeping biological material of part hollow.(see such as Fig. 4 C, its illustrate have by lignin around and the fibre bundle of the cellulose fibre be bonded together but when amplifying, there is the living beings chip of many porous zone.)

After hot water processing section, in chip formation through softening living beings through 1) extruding and 2) and compress be anyly combined into plug form, it is then fed to continous way conveying worm system.Living beings in plug form move in steam blasting section by continous way conveying worm system.Continous way conveying worm system uses the living beings in plug form to prevent from the back-pressure of the blowback of the high steam existed in comfortable steam blasting section to affect hot water processing section.Other method can be used, such as 1) check-valves and 2) segmentation moves living beings, and wherein every section by opening and closing organizational separation.

Steam blasting section still preferably can keep below 450psi up to operation under 850psi.One group of sensor can detect operating pressure.Plug type screwfeed machine transmits chip along steam blasting section.High steam is introduced in plug type screwfeed machine in the section being called steam conveyer.High pressure supply input can be made up of some nozzles that strategy is placed around steam conveyer.The ratio of the living beings chip material be fed to by steam blasting section is accurately controlled via plug type screwfeed machine.The holdup time in steam blasting section is controlled individually by control system.In steam blasting section, living beings in plug form are exposed in the high temperature and high pressure steam from least 160 degrees Celsius of high steam input and 160PSI and continue 5 minutes (and preferably, about 10 minutes), until the integrally-built porous part of moisture penetration living beings and all fluids in living beings and gas rise to high pressure.In an embodiment, steam blasting section has one group of temperature and pressure sensor and control system, continue between 5 minutes to 20 minutes, until the integrally-built porous part of moisture penetration living beings in the high temperature and high pressure steam that wherein living beings are exposed to from least 188 degrees Celsius of the second steam input and 160PSI.

As discussed, when humidity/moisture that system has a certain level in living beings chip is to provide blast source, steam blasting process acts on best.Therefore usual, the moisture of chip is substantially by weight at least 50% to 55% when in steam blasting reactor.In the steam blasting section of steam blasting unit 108, containing having in the room of the living beings chip of softening lignin, pressure and temperature is elevated to the high temperature of rising of at least two ten degree of the operating environment in specific heat hydration process section with the container of living beings chip and the pressure of the rising of higher than the normal pressure in room 14 times, but has shorter duration time period of arranging in specific heat hydration process section.

Living beings in plug form are fed to refining section by steam blasting section by continous way conveying worm system.Steam blasting section is coupled to refining section, refining section has one or more blade, its be configured to be left by outlet opening through Pressed bio matter steam blasting section to maintain lower than pressure in steam blasting section 1/3rd pressure under purge pipeline before mechanically stir through Pressed bio matter so that at internal division through Pressed bio matter.Mechanical agitation in refining section is configured to make gained living beings of a granular form have the more consistent size distribution of the average-size of biological particles.The blade of refining section mechanically stirs through pressurization and moistening living beings and the living beings after stirring are delivered to aperture exit.

In an embodiment, little opening forms outlet and in pipe under entering the pressure maintaining about 4 to 10 bar or other container area, and any internal flow under high pressure or gas expansion are with in internal division living beings.In some cases, from the pressure drop of the high pressure in steam blasting reactor always down to atmospheric pressure.In either case, the larger pressure drop occurred in the outlet in pipe or in steam blasting section and other container between the cyclone section of dewatering declines rapidly.In an embodiment, carry out pressure drop rapidly, method is in the pipe by the overall structure of the living beings between 160 to 450PSI being stretched under significantly decompression (such as 4 to 10 bar), with inside " explosion " the steam rapid expanding caused after pressure decreases or cause owing to liquid water " flash distillation " after being reduced to its vapour pressure under stress becomes steam, the living beings in chip formation are split into living beings fine particle in inside by it.In another embodiment, the steam blasting reactor part of steam blasting section contains special output mechanism, and it is configured to next section under living beings chip material " explosion " to atmospheric pressure.Output mechanism is opened and the living beings from high steam explosion reactor is discharged this reactor and discharges outlet valve or door in the feed line of blowpit.

Therefore, go out the steam blasting reactor in section since then decline rapidly to cause explosion through steam under pressure or superheated water, living beings chip is resolved into fine particle by this.(see such as Fig. 4 D, it illustrates that explosion becomes the living beings chip of living beings fine grained 453.) form the fragment that the pristine fibre bundle Shaping by blast of living beings becomes discrete fine powder granules.(see such as Fig. 4 A to 4C, its illustrate have by lignin around and the difference amplification level of the living beings chip of the fibre bundle of the cellulose fibre be bonded together being formed with Fig. 4 D contrast.)

In the end of container/purge pipeline, moisture and living beings chip are extruded reactor outlet to the container under roughly atmospheric pressure, such as purge pipeline.The high steam of the fiber of part hollow and other inside, porous zone of biological material or water convert steam to and make biomass cells explosion become fine grain moist powder.The overall structure of living beings comprises the organic polymer of lignin and the hemicellulose around multiple cellulose fibre.The overall structure of living beings in this SEP step at internal division, this SEP step uses at least moisture, pressure and heat to discharge and exposed fibers cellulose fiber, (as an example) directly can react during biomass gasification reaction instead of only first react at lignin and hemicellulose layer thus then react after exposed fibers cellulose fiber.High temperature also reduces the energy/power needed for the structure of decomposing biomass, promotes that the lignin along the fiber separation in middle level softens because exist.

Therefore, in inside in steam blasting section, in steam blasting reactor, there is mechanical mechanism opening (such as, valve or door) or only aperture.Reactor is filled with and may softens living beings chip by the warp in plug form at elevated pressures, and by those after softening living beings chip is exposed to low pressure a period of time, for physically the overall structure of the fibre bundle of the living beings containing lignin, cellulose fiber peacekeeping hemicellulose is split into fragment and separated from one another.When in steam blasting reactor under not too exacting terms (such as, 175 to 185 degrees Celsius and 160PSI) when operating steam blasting process, so the particle of fubril chip size to be discharged and (such as, 300PSI) produces extremely meticulous particle under more exacting terms from outlet.

Have from the living beings being produced as moist fine particulate form of described section and be less than 50 micron thickness and the average-size being less than 500 microns long.In an embodiment, steam blasting section is coupled to refining section, refining section has one or more blade, it is configured to mechanically stir through Pressed bio matter before leaving steam blasting section to purge pipeline through Pressed bio matter by outlet opening, and the living beings fine grained with the moisture of reduction produced comprise into cracked, that tear, that tear up and any combination and can have substantially and be less than 30 micron thickness and the cellulose fibre being less than the average-size of 250 microns long.The living beings fine grained of those humidities produced is fed to the feeding district of biomass gasifying furnace 114 subsequently.

The fragment and the fragment that in inside, the overall structure of the living beings in fibre bundle are split into cellulose fibre, lignin and hemicellulose cause following all threes: 1) compared to the living beings in chip formation received, the surface area of the living beings in fine particulate form increases, 2) needs before starting the reaction of cellulose fibre, the skin of lignin and hemicellulose being reacted are eliminated, and 3) viscosity of living beings in fine particulate form changes with as the grains of sand instead of as fiber flow.

The morphologic change to living beings produced by SEP reactor can comprise:

A. complete fibre structure is not had, but all parts explosions thus cause more multilist area, this causes the more high reaction rate in biomass gasifying furnace;

B. fiber presents bending, their layerings, and cell membrane is exposed and breaks;

C. some lignin keep the cell membrane depending on cellulose fibre;

D. hemicellulose is partly hydrolyzed and is partly dissolved together with lignin;

E. the bonding major part between lignin and carbohydrate/polysaccharide (i.e. hemicellulose and cellulose) ruptures; And

F. discussed herein many other changes.

The fine grained of the humidity formed can be such as average diameter 20 to 50 micron thickness and length is less than 100 microns.It should be noted that 1 inch=25,400 microns.Therefore, living beings from average long up to 1 inch during wood chipping equipment unit 104 and 0.25 inch, and become average diameter 20 to 50 micron thickness during fine grained as humidity and length is less than 100 microns as chip, and this reduces in size more than 2000 times.The violent explosion decomposition of saturated living beings chip occurs under the speed can overflowed from the structure of living beings with the saturated high pressure moisture in the porous zone than the living beings in chip formation more rapidly speed.

It should be noted that the exterior mechanical not needing cell or fibre bundle is separated, in fact described process use steam is outside explosion cell from inside.(see Fig. 4 E, it illustrates the living beings chip with mass of fibers that is that be worn or that be partly separated into individuals fibers, living beings chip 451.) in living beings chip, use SEP to produce cellulose and there is the fine particle of hemicellulose of some lignin coatings.(see Fig. 4 D, it illustrates the chip of example living beings, comprises the first living beings chip 451, resolves into living beings fine grained 453.) this is the lignin of fine-grained form, hemicellulose and cellulosic compound have the highdensity high surface that can move in systems in which/transmit.

The living beings fine grained produced is fed to biomass gasifying furnace 114 for the quick bio matter gasification reaction in the reactor of biomass gasifying furnace 114 to downstream, because they form higher surface-to-volume ratio compared to the living beings in chip formation received for the living beings of identical amount, this allows more high heat to be delivered to more rapid thermolysis and the gasification of all molecules in biological material and living beings.

Please refer to Figure 1B, as an example, wherein one or more steam supply input can comprise the low-pressure steam producing the recirculation addle reclaimed since one or more hydrocyclone unit.Such as, embodiment as described herein comprises from hydrocyclone unit derivation waste gas and waste gas is fed to biomass gasifying furnace.Equally, those gases and other condensate any can be fed to turpentine oil recovery unit.Therefore, the gas of the organic compound containing the spin current device unit recovery produced by steam blasting section is collected and is fed to biomass gasifying furnace by feed line.Those gases containing organic compound are then converted to synthesis gas components and other gas by biomass gasifying furnace.

Turpentine oil and other volatile matter can be transported to biomass gasifying furnace via the steam atomization of the dirty condensed water reclaimed from one or more hydrocyclone unit.Such as, the waste gas from one or more cyclone can be comprised containing volatile matter/terebinthine feeding steam and be fed to gasification furnace.Turpentine oil recovery unit and goods for sale, gasification furnace or for the buner system of gasification furnace or reburner can be comprised.In addition, can be recovered in compress living beings time extrude and via the movement of screwfeed system addle and be sent to turpentine oil recovery unit.

In an embodiment, cycling may be used but not continuous conveyor system.Cycling allows soft moist chip to be loaded in SEP reactor and then steam input is introduced high temperature and high pressure steam and continued 10 minutes with the pressure of the gas in elevates biological matter and liquid.After this stage, valve or door are opened biological particles is stretched in feed line in blowpit.

The collecting chamber at the outlet section place of steam blasting section is used for collecting and is reduced to compared with small particle size and in the living beings of slurry form.One or more swirl-type filter can with feed line in line to make steam be separated from biological particles, and wherein biological particles is then fed to blowpit.

It should be noted that and also can be incorporated to method to reduce pressure in the outlet of steam blasting unit thus to reduce power gas.Therefore, one or more reduced pressure zone can be comprised so that the high pressure drop from SEP container is low to moderate lower discharge pressure.Therefore, the design can comprise and in the middle of steam blasting unit, to locate pressure drop position pressure to be low to moderate the decompressions of such as 4 to 10 bar from the high pressure drop steam blasting unit.Pressure drop can be carried out earlier in the duct thus form eddy flow.

Equally, in the exemplary embodiment, biological particles SEP pre-treatment step and gas-entrained biological particles is fed in biomass gasifying furnace between do not have other air to introduce, which reduce radiation and Purge gas.Option can be comprised gas-entrained with what use the power gas that comes from steam blasting unit in biomass gasifying furnace.

In another embodiment, in the exit of steam blasting section, the once explosion of the living beings in plug form becomes moist fine particulate form.The steam blasting section being filled with high steam and/or superheated water contains discharges outlet, and it is configured to the living beings that next section arrived by biological material " explosion " is at atmosheric pressure fine particulate form with generation.Living beings in fine particulate form flow through the feed line of blowpit under high speed.

Living beings in moist fine particulate form enter the feed line of blowpit.Feed line is originally less, such as diameter only 1.5 inches, and wherein biological particles passes through under high speed.Can add flow enhancing agent in the initial part of purge pipeline, such as wax, fiber is still moistening to improve material uniformity and to avoid waterpower to bond simultaneously.It is 60 inches that present feed line is expanded to diameter, and the living beings in moist fine particulate form are by maintaining its heat around the heater coil arranged and heat purge pipeline.Maintain the temperature of living beings often help the rosin of living beings with resin acid crystallization thus prevent conglomerate together with fiber grain.Therefore, temperature contributes to preventing lignin from luming and preventing rosin from hardening.

Comprise 1) from the recirculation ashes and 2 of biomass gasifying furnace 114) glidant of any one in alkene (such as, wax) is 1) the discharge outlet and 2 of steam blasting section) any one place's injection in feed line to be to prevent from being blocked by living beings.In addition, feed line can have the heater coil that arranges around feed line to maintain the high temperature of living beings in fine particulate form, thus helps prevent the crystallization of rosin in the living beings in fine particulate form and resin acid.

The biological particles produced is owing to steam flash distillation being discharged and the larger percentage of the content that dries out as steam in purge pipeline.The biological particles produced and moisture are then separated by swirl-type filter and are then fed to blowpit.Therefore, water separative element is embedded with purge pipeline.The collecting chamber at the outlet section place of steam blasting section is used for collecting and is reduced to compared with small particle size and is the living beings of slurry form and is fed to water separative element.Water is removed from the living beings in fine particulate form in hydrocyclone unit and/or dryer unit.

The fine grain moisture of living beings is become dry by dryer unit (such as, flash dryer or low-temperature bake unit) in the exit of blowpit further, and fine grain for living beings moisture is reduced to by weight lower than 1% to 20% by this.Target prepared by fiber be formed following biological particles: its have maximized surface amass and be dried to as far as possible exported living beings fine grain by weight 5% to 20% moisture.Flash dryer only blows out hot-air with the biological particles of drying from blowpit.Flash dryer can be positioned at the exit of blowpit substantially or substitute cyclone in its porch, contains be greater than the moisture that 5% is still less than 20% by weight to make exported biological particles.Living beings can be fed to silo and be used for storing to make SEP living beings fine grained become dry before being fed to lock hopper further by flash dryer.In an embodiment, speed when paddle drier can enter drier owing to the gas of load bearing grain further and reduce biological particles size, it serves as the grinder for the biological particles entered.

The difference of gained biological particles and thermomechanical pulping (TMP) is that particle easilier than the fiber be often wound around and lump to flow as crystal structure.

Living beings in fine particulate form by weight 5% to about 35% the moisture of minimizing be fed to roasting unit 112 by induction system (as an example), thus roasting or pyrolysis is being experienced at the temperature of 100 to 700 degrees Celsius, continue preset time quantum.

Living beings of a granular form are fed to roasting unit 112 to process living beings at lower than the temperature of 700 degrees Celsius by conveyer system, continue preset time quantum to form waste gas, by create collected by storage tank and finally can be fed to the synthesis gas components of organic liquid goods synthesis reactor (such as, methanol synthesis reactor) a part of time use.

The living beings fine grained coming from blowpit and flash dryer has had low moisture content owing to steam flash, further air oxygen detrition, and is the compound of the fragment of the cellulose fibre of the fragment with lignin coating, lignin, cellulose and hemicellulose etc.Biomass gasifying furnace 114 has reactor vessel, and its living beings in moist fine particulate form being configured to the surface area making to have increase react owing to the division by steam blasting unit 108.Biomass gasifying furnace 114 has high steam supply input and one or more heater, and depositing in the case of steam, living beings in fine particulate form to react with quick bio matter gasification reaction with the holdup time between 0.1 second and 5.0 seconds thus produce at least synthesis gas components in reactor vessel, comprise hydrogen (H2) and carbon monoxide (CO).When produced fine grained is fed to biomass gasifying furnace 114 with high density, then granule reacts and more easily and up hill and dale the larger hydrocarbon molecule of living beings is resolved into synthesis gas components fast.Therefore, nearly all biological material lignin, cellulose fiber peacekeeping hemicellulose gasify up hill and dale, but not the same range that some the undecomposed sclerderm shells to coking chip in the interior section of chip decompose.These fine graineds form less residu tar, less carbon coating and less sediment compared to chip.Therefore, the integrated morphology smashing the living beings in fibre bundle often reduces the amount of the follow-up tar produced in gasification of biomass.These fine graineds also allow the material of larger bulk density to be fed to biomass gasifying furnace 114.As note, the water with by weight at least 10% can assist the methyl alcohol CH30H of generation except CO and H2 produced in biomass gasifying furnace 114 as product as liquid or steam.

Roasting unit and biomass gasifying furnace 114 can be combined as integral unit.

In replacement scheme, moist directly or after drying can be fed to granulator from the output of steam blasting reactor in slurry form through division biological particles.Living beings can be become biological particles from fine particulate form densification by granulator, and those particles are then fed to biomass gasifying furnace.Living beings this direct feeding from fine particulate form to particle form saves many steps and a large amount of energy consumptions relevant with those removal process with conversion.Alternatively, particle can be transmitted to facility for being further processed as liquid fuel, heat/electric power, animal feed, bedding and padding or chemicals.

In an embodiment, biomass gasifying furnace 114 is designed to radiation ground transfer of heat to the biological particles flowing through reactor design, and wherein the Quick-gasifying holdup time of biological particles is 0.1 second to 10 seconds, preferably, is less than one second.The radiant heat on biological particles and the reacting gas surface of origin autoradiolysis thermal reactor substantially of flowing through radiant heat reactor promotes and the particle may carried secretly in heat trnasfer ground auxiliary flow.Reactor can with generally more than 900 degrees Celsius and preferably the heating temperatures particle of at least 1200 DEG C to produce the synthesis gas components comprising carbon monoxide and hydrogen, and under produced methane is remained on exiting goods, exit minimum tar residual in goods and the level of the <1% of the component composition of ashes that produces.

Fig. 3-1 to 3-4 shows the exemplary embodiment of biomass gasifying furnace 114.Fig. 3-1 shows and uses photothermal fountain reactor, and the gas-entrained bottom place at gasification furnace wherein carrying living beings is entered and projected by central tube and the fountain above the partition wall formed by central tube and fall within the section formed between outer tube and central tube.Fig. 3-2 and 3-3 shows the design of exemplary bayonet socket reactor radiant heat, and wherein a series of radiant heat is effective in heat the living beings injected.Heat directly can be provided to pipe or be provided to the intermediary source being fed to pipe, such as heated air by gas burner.Living beings can be outside at pipe, and heat is fed to pipe in inside.Alternatively, living beings can between tube sheet and refractory lining.Fig. 3-4 shows exemplary downdraft radiant heat reactor, wherein multiple effective in provide radiant heat to reactor.Living beings can or pipe is outside, heat is fed to pipe in inside, or vice versa.

Hot receiver 106 has the chamber with inwall.Multiple pipes 102 of chemical reactor are positioned to skew and the interlaced arrangement in receiver 106 inside by the geometry promoted relative to the radiation of the chamber wall of the hot receiver 106 of reaction tube 102.The surface area of chamber wall is greater than the area that reaction tube 102 takies and arrives the region pipe 102 to allow radiation from multiple angle.The inwall in receiver 106 chamber and reaction tube 102 are basically by the radiation exchange energy, its mesospore and pipe 102 serve as the transmitter again of radiation to obtain the heat flux of the high radiation arriving all pipes 102, and therefore, avoid shielding and block radiation to arrive pipe 102, thus allow reaction tube 102 to obtain from the reaction zone in reaction tube 102 to the extremely consistent Temperature Distribution ended up.

Therefore, the geometry of reaction tube 102 and chamber wall makes the distribution of incident radiation be shaped in the following manner: use these 1) the staggered and pipe 102 of skew, it is in conjunction with 2) compared to the chamber wall of the area larger diameter shared by annex pipe 102, and other 3) be combined in mutual pipe radiation exchange between geometry place multiple reaction tube geometrical arrangements relative to each other.Wall is by high reflection radiation or absorb and the material of emitted radiation is again made.The distribution of incident radiation moulding be used in the intracavitary irradiation of receiver 106 reflection and both absorbing.Therefore, the inwall of hot receiver 106 by or 1) absorb and emitted radiation energy again, 2) by incident radiation high reflection to pipe 102, or 3) these any combination aims at and serves as radiation distributor, thus maintaining the operating temperature of annex excessive heat flux chemical reactor.Serve as the transmitter again of radiation from 1) chamber wall, 2) directly from heat-storage type burner and 3) adsorbed by reaction tube 102 from the radiation of the outer wall of other pipe, and then heat is by being delivered to the inwall of reaction tube 102, wherein at the temperature of heat between 900 degrees Celsius and 1600 degrees Celsius (and preferably, higher than 1100 degrees Celsius) be radiated reaction particles and gas.

As discussed, the inwall in the chamber of receiver 106 and reaction tube 102 exchange the energy mainly through radiation instead of by convection current or conduction among each other, thus allow reaction tube 102 to obtain extremely consistent Temperature Distribution, even if general lower temperature biological particles and gas-entrainedly enter reaction tube 102 in the reaction region from the first entrance and through the chamber through heating to leave reaction zone at the second exit point.This radiant heat transmission from inwall and reaction tube 102 promotes chemical reaction and makes the temperature fast lifting of chemical reactant to the temperature of other discharge material close to goods and disengaging reactor outlet.

The length in the gasification reaction district of each in reaction tube 102 and diameter dimension through setting size to be greater than the outlet of the holdup time of 0.1 second and the gasification zone in multiple reaction tube 102 under the gasification temperature being given at least 900 degrees Celsius.Product has the equaling or exceed the temperature of 900 degrees Celsius of outlet from gasification zone, and the multiple reaction tubes 102 in the design of this chemical reactor increase the available reactor surface area of radiation exchange for biological particles and inner room radiation exchange.The Quick-gasifying of the living beings particulate fallen and the stable ashes of gained that dispersion occurs in reaction tube 102 in reaction zone within the holdup time are formed, thus make the complete of tar be improved as every standard cubic meter lower than 500 milligrams, and the living beings of at least 90% are converted to the production of hydrogen and carbon monoxide goods.

In order to realize high-conversion rate and selection rate, gasification of biomass requires that temperature is more than 1000 DEG C.These are difficult to realize in the fluidized bed gasification furnace of standard, because higher temperature requires the burning of the constantly larger part of living beings itself.Therefore, indirect and fluidized bed gasification is limited to the temperature of 800 DEG C usually.At these tem-peratures, the generation of undesirable higher hydrocarbon (tar) is obvious.These tar clog downstream equipment and make catalytic surface dirty/passivation, thus in tar removing equipment, need a large amount of capital investments (10% to 30% of total equipment cost).High heat-flux hot systems can obtain high temperature in pole efficiently.The more important thing is, can according to the efficiency of concentration and temperature required control procedure, and realize high temperature and no longer need loss biomass portion.Therefore, the temperature in tar cracking situation (1000 to 1300 DEG C) can be realized, and can not the fuel that produces from living beings of loss or overall process efficiency.This eliminate the complicated tar cracking equipment be usually associated with biomass gasification system to arrange.In addition, the heat trnasfer of operations improvement at high temperature and decrease the required holdup time, thus reduce the size of chemical reactor and decrease its fund cost.

And the operating temperature that the wall temperature between 1200 DEG C and 1450 DEG C is clear delimitates and usually not occurring in gasification higher than the temperature of exhaust gas of silica fusion temperature (1600 DEG C) more than 900 DEG C, and not appearance in (circulation of fluid bed) gasification indirectly certainly.The common gasification of living beings can carried out in excessive heat flux chemical reactor and the possibility of the steam-reforming of natural gas can not occur in partial oxidation gasification furnace (because methane is by preferential combustion).The flexibility of process raw material comes from simple tubular design, and for reason discussed herein, most of gasification furnace cannot process the fuel of different range.

The material of inwall forming receiver 306 chamber can have machinery and chemical attribute to keep its structural strength under the high temperature between 1100 DEG C to 1600 DEG C, for receiver 306 chamber, there is the high radiance of ε >0.8 or the high reflectance of ε <0.2, and high heat capacity (>200J/kg-K) and lower thermal conductivity (<1W/m-K).The material forming reaction tube 302 has the high heat capacity (>150J/kg-K) of high radiant rate (ε >0.8), high heat conductance (>1W/m-K), appropriateness.

In order to determine that the case granularity analysis of granular size can be Digital Image Processing granular size and shape analyzing system, such as, the CamsizerXT Particle Size Analyzer of Ku Chang Group Co., Ltd (Horiba, Ltd.).This type systematic uses one or more camera to think, and dry powder in the magnitude range of (such as, from 30 μm to 30mm) and bulk material provide granularity fast and accurately and grain shape distribution.Measurement from digital image processing system allow existing data with screen and deposit (it also can be used for measuring granularity in some cases) and equally have all different technology to be associated.In an embodiment, the granularity of the wood chip of the CamsizerXT particle size analyzer steam blasting of Ku Chang Group Co., Ltd (Horiba, Ltd.) is used.Sample to be measured is mediated by external control in the bag that can repeat sealing and the material stirred in bag mixes.After blending, such as roughly the sample size of 3cm^3 is loaded into the sample hopper of instrument.Target runs and analyzes enough sample sizes, and such as, at least from 200 ten thousand particles of each sample, therefore sample volume is uniquely important with regard to this degree, because it is equivalent to the particle of sufficient number.Example settings on instrument can be as follows: area coverage, the image rate 1:1 of 0.2%, have X-injection, gap width=4.0mm, dispersive pressure=380.0kPa, xFe_max [and correspondingly xc_min].Controlling feeding ratio makes computer can process image enough rapidly to produce target coverage area.Camera imaging ratio is fixing, and obtains " substrate " image and zoom image for each run.The single value of particle mean size, such as diameter is less than 50 microns, can be objective measurement standard.In an embodiment, three point values of Fe-max and xc-min are more complete.Therefore, seem as 6 point values.Size distribution (PSD) can be defined as Fe-MaxD10, D50, D90 and Xc-minD10, D50, D90.Then measure and multiple value (such as, inputting 6 values) can be used to determine measured value.Other similar means can be used.

Femax and xcmin based on volume can be used to calculate.Two models can be used to carry out analysing particulates image: xc-min, it produces the result suitable with those results obtained by examination/Screening Samples for physically; And Fe-max, it is similar to the longest dimension with the given particle of kind of calliper.Initial data, frequency diagram is obtained, the result of sealing up for safekeeping and particle image for all samples.D10, D50 and D90 can calculate based on volume, are average aspect ratios.D90 describes the percentage 90 wherein distributed and has smaller particle size and percentage ten has diameter compared with coarsegrain.It is less larger with percentage 90 that D10 diameter has percentage ten.Three of D10, D50 and D90 specifications are provided to be regarded as complete and to be suitable for most of granular materials.In an embodiment, size distribution PSD can be defined as D50 (μm) model Fe-max.

table 1-is for the size distribution of the timber of steam blasting

The fineness number of the sample of SEP process is produced by xc-min and Fe-max model.

The example in table 1 is produced by the steam pressure of 16 bar and the reaction time of 10 minutes.

Fig. 2 shows in order to produce synthesis gas and produce the embodiment of the flow chart of the integrated equipment of liquid fuel goods from living beings from synthesis gas.Steam blasting unit 308 can have steam blasting section and hot water processing section, and it is fed to by biological particles or drier, roasting unit or be directly fed to biomass gasifying furnace 314.Drier can be flash dryer, rotary drum drier, pedal-type dryer, air dryer or similar such device.

In an embodiment, induction system is coupled to the collecting chamber at the outlet section place at steam blasting unit 308, and living beings of a granular form are fed to by cyclone or roasting unit 312 or be directly fed to biomass gasifying furnace 314, or are fed to flash dryer.The most of original wood element and the cellulose that form living beings in the receiver section of the steam pipeline section in steam blasting unit 308 remain produced biological particles, but are separated with the cellulose fibre in the collecting chamber at the outlet section place of steam blasting section 308 haply now.

From the non-condensable hydrocarbon produced from any waste gas of living beings during collecting chamber in steam blasting unit 308 is configured to be collected in steam blasting process.

After steam blasting section 308, at water separative element (such as, hydrocyclone unit) in remove water from living beings, and the living beings of the reduction moisture be made up of lignin and the cellulose of the fiber relaxed and separation can be fed to drier.

In an embodiment, from producing from the non-condensable hydrocarbon of any waste gas of living beings and those non-condensable hydrocarbons being delivered to catalyst 316 together with any material collected in roasting unit 312 during the one or more gas collection casees in steam blasting unit 308 can be collected in SEP process.

In another embodiment, the slurry reducing moisture directly can go to biomass gasifying furnace 314, roasting unit 312 or catalyst 316 from steam blasting unit 308.Usually, the particle of living beings goes to roasting unit 312 and then on biomass gasifying furnace 314.But roasting unit 312 and biomass gasifying furnace can be combined into individual unit.

Can the general composition of biomass type of fusion such as comprise:

Biomass gasifying furnace 314 has reactor, and it is configured to make the biological particles decomposed by two sections of steam blasting unit 308 or more sections to react and those biological particles are fed to the feeding district of biomass gasifying furnace 314 subsequently.Biomass gasifying furnace 314 has high-temperature steam supply input and one or more heater, and depositing in the case of steam, the biological particles decomposed by steam blasting unit 308 in reactor vessel to react with quick bio matter gasification reaction at higher than the temperature of 700 degrees Celsius in the holdup time being less than five seconds in biomass gasifying furnace 314 thus to produce at least synthesis gas components, comprise hydrogen (H2) and carbon monoxide (CO), it is fed to methyl alcohol (CH3OH) synthesis reactor 310.In gasification furnace 314, the heat being delivered to the biological particles be made up of the fragment of the cellulose fibre loosened, lignin and hemicellulose or cellulose fibre, lignin and hemicellulose no longer needs infiltration lignin and hemicellulose layer to arrive fiber.In certain embodiments, quick bio matter gasification reaction carries out guaranteeing during gasification reaction, form minimum tar at higher than the temperature of 700 degrees Celsius.Therefore, 700 degree initial temperature but may be the obvious scope of gasification of biomass furnace operating lower than 950 degree.Make all gasification of biomass more thoroughly and easier.

Biomass gasifying furnace 314 can have to flowing through the particle of reactor design with the Quick-gasifying holdup time of biological particles (0.1 second of biological particles by 10 seconds and be preferably less than Quick-gasifying holdup time of one second) and flowing through the radiant heat transmission of reacting gas of radiant heat reactor, and from the surface of radiant heat reactor and the main radiant heat of particle carried secretly in flowing by particle and gained gas-heated to beyond roughly 700 degrees Celsius and the preferably temperature of at least 1200 DEG C, to produce the synthesis gas components comprising carbon monoxide and hydrogen, and produced methane is remained on and exits goods, under exiting the level of the <1% of the component composition of the minimum tar remained in goods and the ashes produced.In certain embodiments, the temperature range for gasification of biomass is higher than 800 degrees Celsius to 1400 degrees Celsius.

With reference to figure 2, any combination of equipment use three kinds of modes is to produce the synthesis gas being used for methanol production.Synthesis gas can be the mixture of carbon monoxide and hydrogen, and it can convert the large weight organic compounds being suitable for and making chemicals raw material, fuel and solvent to.Such as, biomass gasifying furnace 314 make living beings gasify at sufficiently high temperature to eliminate generation hydrogen and carbon monoxide for during methanol production to the needs of catalyst.

Gasification of biomass is used for the complicated hydro carbons of living beings being resolved into simpler gaseous molecular, mainly hydrogen, carbon monoxide and carbon dioxide.Also form some mineral ashes and tar, and methane, ethane, water and other component.Elementary goods mixture change according to the type of used biomass material and the gasification process that uses.

Biomass gasifying furnace is followed by gas purification section to clean ashes, sulphur, water and other pollutant from synthesis air-flow of exiting biomass gasifying furnace 314.Synthesis gas is then compressed to for the suitable pressure needed for methanol-fueled CLC.Other synthesis gas from steam methane reforming stove 327 can connect upstream or the downstream of compression section.

Forming gas from H2 and CO of gasification furnace and steam methane reforming stove 327 is sent to public input to one or more methanol synthesis reactor.To be received the analysis of the composition of the synthesis gas exiting biomass gasifying furnace 314 and steam methane reforming stove 327 from monitoring equipment by control system and make to optimize ratio to methanol-fueled CLC, can the precise proportions of Optimization of Hydrogen and carbon monoxide.The methyl alcohol produced by one or more methanol synthesis reactor is then processed in the process of methyl alcohol to gasoline.

The liquid fuel produced in integrated equipment can be gasoline or other, such as diesel oil, jet fuel or some alcohols.

Therefore, biomass gasifying furnace 314 and SMR327 can be used for and answer synthesis gas components to downstream organic liquid goods synthesis reactor, such as methanol synthesis reactor 310.Then methyl alcohol is fed to methyl alcohol to gasoline process to form high-quality and high-octane gasoline.Methyl alcohol also can be used for other liquefied fuel process required, comprises jet fuel, DME, gasoline, diesel oil and mixed alcohol.

Fig. 4 A to Fig. 4 C show have by lignin around and the difference amplification level of the example living beings chip 451 of the fibre bundle of the cellulose fibre be bonded together.

Fig. 4 D shows the example living beings chip that explosion becomes living beings fine grained 453, comprises the first living beings chip 451.

Fig. 4 E shows the living beings chip 451 with mass of fibers that is that be worn or that be partly separated into individuals fibers.

Fig. 5 shows the flow schematic diagram of the embodiment of the radiant heat chemical reactor being configured to produce the chemicals comprising forming gas product.Many shells radiant heat chemical reactor 514 comprises the refractory container 534 with annular chamber, and annular chamber has inwall.Radiant heat chemical reactor 514 has two or more radiant tubes 536 be made up of solid material.The chamber that one or more radiant tube 536 is positioned at the container 534 of band refractory lining is inner.

The thermal source 538 of heating heats the interior volume of pipe 536.Therefore, the thermal source 538 (such as, heat-storage type burner or gas burner) that each radiant tube 536 is used in the heating of each end of pipe 536 heats from inside.Each radiant tube 536 is by the heat insert port of each end of pipe 536 and heated from inside by the one or more heat insert ports fire between two ends and the gas from burner possibly.The flame of one or more Natural Gas burner 538 and serve as the thermal source of heating through heated air, is fed to multiple radiant tube at its temperature between 900 DEG C and 1800 DEG C and is connected to two ends of radiant tube 536.Each pipe 536 can be made up of SiC or other similar material.

In the top that living beings and reacting gas are fed to chemical reactor 514 by one or more feed line 542 or upper part.For entering below entrance in the container 534 of the band refractory lining of the radiant tube 536 for heating in inside of the feed line 542 of biological particles and steam.Feed line 112 is configured to comprise 1) biological particles, 2) reacting gas, 3) steam, 4) heat trnasfer auxiliary particle or 5) chemical reactant of any one in above-mentioned four kinds is fed in radiant heat chemical reactor.Multiple radiant tubes 536 outside that the chemical reaction promoted by radiant heat has inner fire is carried out.The chemical reaction promoted by radiant heat is carried out in the outer wall of each in the inwall and one or more radiant tube 536 in the chamber of the container 534 of band refractory lining.

Chemical reaction can be comprise 1) gasification of biomass (CnHm+H2O → CO+H2+H2O+X) and 2) one or more endothermic reaction in other similar hydro carbons decomposition reaction, it uses radiant heat to carry out in radiant heat chemical reactor 514.The mol ratio of steam (H2O) and charcoal is in the scope of 1:1 to 1:4, and temperature is enough high to carry out chemical reaction in the absence of a catalyst.

To the raw-material biological particles that is used as in the design of radiant heat reactor, there is following advantageous effects: improve by more effectively radiant heat being delivered to particle that gas carries secretly and the process gas temperature more than 1200 degrees Celsius can be maintained, gasification furnace yield that the living beings feeding for specified rate improves the synthesis gas components producing carbon monoxide and hydrogen and via reducing the generation of tar and C2+ alkene and improving technique health.Control system for radiant heat reactor makes the flow rate of the radiant heat coupling biological particles transmitted from the surface of reactor to produce above advantage.

Control system controls gas burner 538 to supply heat energy to chemical reactor 514, thus helps the radiant heat that chemical reactor is produced to have high heat-flux.The inner surface of chemical reactor 514 is through aiming at 1) absorb and emitted radiation energy, 2 again) high reflection emittance and 3) these any combination, thus maintain the operating temperature of annex excessive heat flux chemical reactor 514.Therefore, the outer wall emitted radiation heat energy of each in the cavity wall of refractory container and one or more pipe 536 is to (such as) biological particles and other heat trnasfer auxiliary particle any of existing between the outer wall giving fixed tube 536 and the inwall of refractory container.Therefore, refractory container absorbs via pipe 536 from the burner 538 along the top of refractory container and location, bottom or reflect and concentrates the energy to cause the energy source by heat radiation and reflection, thus heat flux is transported to substantially the biological particles of chemical reactor inside, heat trnasfer auxiliary particle and reacting gas.The inwall in the chamber of insulating refractory container and multiple pipe 536 by or radiation-absorbing it is radiated heat trnasfer auxiliary particle again or reflecting incident radiation is served as radiation distributor to heat trnasfer auxiliary particle.Radiant heat chemical reactor 514 uses the excessive heat flux and high temperature that promote mainly through the heat trnasfer of radiation instead of convection current or conduction.

In coal particles, normally used convection current biomass gasifying furnace arrives at most the heat flux of 5 to 10kW/m^2 usually.High radiation heat flux biomass gasifying furnace will use obviously larger heat flux, be those amounts existed in the biomass gasifying furnace of convection current promotion at least three times (that is, higher than 25kW/m^2).Usually, at high temperature (wall temperature >950 degree Celsius) uses radiation, can realize higher flux (high heat-flux higher than 80kW/m^2) with the reactor suitably designed.In some cases, high heat-flux can be 100kW/m^2 to 250kW/m^2.

Next, in the general situation of the computer executable instructions performed by computer, (such as, program module) be used for control system various algorithm and method can be described.Usually, program module comprises routine, program, object, assembly, data structure etc., and it performs particular task or implements concrete abstract data type.Description herein and/or figure can be embodied as computer executable instructions by those skilled in the art, and it can implement on any type of computer-readable media hereafter discussed.In general, program module may be embodied as software instruction, the logical block of electronic hardware and both combinations.Software section can be stored on machine-readable medium and to write with the programming language of any number, such as Java, C++, C etc.Machine-readable medium can be hard disk drive, peripheral driver, DRAM, magnetic tape station, memory stick etc. but not contain instantaneous signal.Therefore, hardware logic, hardware logic and software interactive effect can be used uniquely or only use software construction algorithm and control system.

But some specific embodiments of the design have shown that the design is not limited to these embodiments.Such as, pre-heated combustion air or may be used for other similar heater can be used for from the recovery used heat of various device procedures.Heat accumulating type gas burner or normal burner can be used as the thermal source of boiler.Steam methane reformingly can be/comprising SHR (steam hydrocarbon performer furnace), it makes to comprise hydro carbons (alkane, alkene, alkynes, aromatics, furans, phenols, formic acid, ketone, aldehydes, ether etc.) and the short-chain hydrocarbons (<C20) of oxygenate splits into synthesis gas components.The design should be understood to not limit by specific embodiment as herein described, but limits by means of only the scope of appended claims.

Claims

1., in order to produce an integrated equipment for synthesis gas from living beings, it comprises:

Steam blasting unit, it has to receive the input cavity that living beings chip is used as raw material, one or more steam supply input, and in order to living beings described in pretreatment for follow-up two sections that are fed to biomass gasifying furnace or more sections, wherein said two sections or more sections use the heat being applied to described living beings, the combination of pressure and moisture is with the fine particulate form making described living beings become humidity, the overall structure of the living beings chip received described in wherein said two sections or more sections are configured to decompose at least in part, method be by application from the first steam supply input steam with start to be reduced in lignin and from the cellulose fibre of described living beings hemicellulose between bonding and the moisture of the living beings chip received described in improving, and the steam then applied in the segment from least atmospheric pressure 14 times of the second steam supply input heats any gas of described living beings inside existence and fluid and pressurizes, wherein at the outlet opening place to described two sections or more sections, via the reduction of blood pressure in high-speed of described living beings described in internal division through the described overall structure of Pressed bio matter, described living beings wherein after division produce and are less than 70 micron thickness and the fine particulate form being less than the average-size of 500 microns long from described section of having of leaving, and the living beings fine grained of those humidities produced is fed to the feeding district of described biomass gasifying furnace subsequently, and

Wherein said biomass gasifying furnace has reactor vessel, it is configured to the living beings of the fine particulate form of described humidity are reacted, the living beings of the fine particulate form of described humidity have the granular size of reduction and the overall surface area increased owing to the division by described steam blasting unit compared to the living beings chip received described in described input cavity, wherein said biomass gasifying furnace has the 3rd steam supply input and one or more thermal source, and when there is described steam, the living beings of described fine particulate form react with quick bio matter gasification reaction thus produce at least synthesis gas components in described reactor vessel, comprise hydrogen (H2) and carbon monoxide (CO), wherein said steam blasting unit and described biomass gasifying furnace are parts for described integrated equipment.

2. integrated equipment according to claim 1, described two sections of wherein said steam blasting unit or more sections comprise at least hot water processing section and steam blasting section, wherein said hot water processing section has the described input cavity receiving described living beings chip, and described first steam supply input is configured to be applied to by low-pressure saturated steam under higher than 60 degrees Celsius but lower than the high temperature of 145 degrees Celsius under the pressure of about normal pressure PSI in the container containing described living beings chip, thus start to decompose, the living beings chip received described in hydration process also softens, wherein the high temperature of one group of temperature sensor to the described living beings chip received provides feedback, and wherein control system is configured to holdup time of keeping described living beings chip to stop in described hot water processing section 8 to 20 minutes, described holdup time long enough soaked into described living beings chip with moisture before being moved out to described steam blasting section in described living beings.

3. integrated equipment according to claim 2, wherein said hot water processing section will be fed to described steam blasting section through softening and that moisture improves described living beings chip via screwfeed system, described steam blasting section maintains the pressure of 10 to 30 times of the pressure existed in described hot water processing section by described control system under, and described steam blasting section raises the internal pressure of the described moisture of described living beings and the cell of the described living beings of formation further.

4. integrated equipment according to claim 1, wherein after described hot water processing section, described in chip formation through softening living beings through 1) extruding and 2) and compress be anyly combined into plug form, it is then fed to continous way conveying worm system, the described living beings in plug form move in steam blasting section by described system, wherein in described continous way conveying worm system, the described living beings in described plug form prevent from the back-pressure of the blowback of the high steam under at least ten four times of the normal pressure existed in comfortable described steam blasting section to affect described hot water processing section, and

The described synthesis gas components comprising described hydrogen (H2) and described carbon monoxide (CO) wherein from described biomass gasifying furnace is fed to downstream methanol synthesis reactor to form methyl alcohol, and described reactor is also a part for described integrated equipment.

5. integrated equipment according to claim 4, wherein said steam blasting section is coupled to refining section, described refining section has one or more blade, its be configured to described through Pressed bio matter to be left by described outlet opening described steam blasting section to maintain lower than pressure in described steam blasting section 1/3rd pressure under purge pipeline before mechanically stir described through Pressed bio matter so that through Pressed bio matter described in internal division, described mechanical agitation wherein in described refining section is configured to make gained living beings of a granular form have the more consistent size distribution of the average-size of described biological particles.

6. integrated equipment according to claim 2, wherein said steam blasting section has one group of temperature and pressure sensor and described control system, wherein said living beings are exposed to and continue between 5 minutes to 20 minutes in the high temperature and high pressure steam from described second steam supply at least 188 degrees Celsius of input and 160PSI, until the integrally-built porous part of living beings described in moisture penetration and all described fluid in described living beings and gas rise to described high pressure, wherein described living beings are fed to described outlet opening by described steam blasting section by conveyer system, the little opening of wherein said outlet opening enters in the pipe under the decompression maintaining 4 to 10 bar, and any internal flow under described high pressure or gas expansion are to split into the fine grained living beings of described humidity by the described overall structure of described living beings in inside.

7. integrated equipment according to claim 1, described two sections of wherein said steam blasting unit or more sections comprise hot water processing section and steam blasting section, wherein said hot water processing section has first group of temperature sensor and control system, it is configured to via described first steam supply input, described steam is applied to described living beings chip at the temperature of the glass transition point higher than described lignin, to soften and to improve the described moisture of described living beings, therefore at least described in described steam blasting section, the described cellulose fibre of living beings can from described living beings at internal division, wherein said hot water processing section is configured to receive described living beings chip, it can comprise leaf, needle, stem skin and bole, and then described control system uses described steam that the described living beings chip in described hot water processing section is heated to above 60 DEG C, be detained the time of 8 to 20 minutes, and then described living beings are delivered to described steam blasting section with other inside, porous zone formation high steam in the described overall structure of biological material described in the cellulose fiber peacekeeping of part hollow, and then make the environmental pressure of the described outlet opening through described steam blasting section decline fast, method is to cause Internal explosions in the pipe by the described overall structure of the described living beings maintained 160 to 450PSI by the described control system in described steam blasting section being stretched under reduced pressure, described living beings are split into living beings fine particle in inside by it, wherein in inside, the described overall structure of the living beings in fibre bundle is split into cellulose fibre, the fragment of lignin and hemicellulose and fragment cause following both: 1) compared to described receive in the living beings of chip formation, the surface area of the described living beings in fine particulate form increases, and 2) structure of the living beings produced in fine particulate form of described gained changes with as the grains of sand instead of as fiber flow.

8. integrated equipment according to claim 1, described two sections of wherein said steam blasting unit or more sections comprise hot water processing section and steam blasting section, wherein at the described outlet opening place of described steam blasting section, once described living beings explosion becomes the fine particulate form of described humidity, then described produced biological particles is owing to steam flash distillation being discharged and the percentage of the content that dries out as steam in purge pipeline, wherein said produced biological particles is then separated by swirl-type filter with moisture, the fine grain described moisture of wherein said living beings is become dry by drier in the exit of purge vessel further, fine grain for described living beings moisture is reduced to by weight lower than 20% by this, the described living beings fine grained with the moisture of reduction is then fed to silo for storage until be ready to be fed to described biomass gasifying furnace by wherein said drier.

9. integrated equipment according to claim 1, wherein steam blasting section is coupled to refining section, described refining section has one or more blade, its be configured to described mechanically stirred before Pressed bio matter leaves described steam blasting section to purge pipeline by described outlet opening described through Pressed bio matter, and described the produced living beings fine grained with the moisture of reduction comprises into cracked, tear, that tear up and any combination and have and be less than 30 micron thickness and the cellulose fibre being less than the average-size of 200 microns long, wherein said produced living beings fine grained is fed to described biomass gasifying furnace for the described quick bio matter gasification reaction in the described reactor vessel of described biomass gasifying furnace to downstream, because they form higher surface-to-volume ratio compared to the described living beings in chip formation received for the living beings of identical amount, this allows higher heat and quality to be delivered to more rapid thermolysis and the gasification of all molecules in described biological material and described living beings.

10. integrated equipment according to claim 2, the described steam blasting section being wherein filled with the high steam be greater than under 14 bar contains discharges outlet, it to be configured to described biological material " explosion " under reduced pressure next section to produce the described living beings in fine particulate form, wherein magnetic filter and air cleanness filter system, coupled to described hot water processing section to guarantee that the described living beings in chip formation eliminated metal fragment and ratchel before entering described hot water processing section, to prevent these metal fragments and ratchel blocking from comprising described part of discharging the described steam blasting unit of outlet, the wherein said living beings in fine particulate form are in the dirty feed line crossing purge vessel of high speed, and 1) the described of described steam blasting section discharge outlet and 2) any one in described feed line locate injection and comprise 1) charge of flowable solids and 2) obstruction that causes to prevent described living beings of the glidant of any one of gas, and other described feed line has the heater coil that arranges around described feed line to maintain the high temperature of the described living beings in fine particulate form thus to help prevent the crystallization of rosin in the described living beings in fine particulate form and resin acid.

11. integrated equipments according to claim 1, it comprises further:

Water separative element, collecting chamber wherein at the outlet section place of steam blasting section is reduced to compared with small particle size in order to collect and is the described living beings of slurry form and is fed to described water separative element, wherein in hydrocyclone unit, removes water from the described living beings in fine particulate form and the described living beings in fine particulate form is fed to drier to be reduced to by weight lower than 20% by the moisture of the described living beings in fine particulate form further; And

Gas wherein containing the organic compound reclaimed from described hydrocyclone unit produced by described steam blasting section is collected and is fed to described biomass gasifying furnace by feed line.

12. 1 kinds in order to produce the method for synthesis gas from the living beings in integrated equipment, it comprises:

The living beings received in chip formation are used as raw material and are fed to biomass gasifying furnace with living beings described in pretreatment in two sections or more sections for follow-up;

By heat in described two sections or more sections, the fine particulate form that the Combination application of pressure and moisture becomes moist to described living beings to make described living beings, steam blasting process wherein in described two sections or more sections decompose at least in part described in the overall structure of the living beings in chip formation that receives, method be the steam that there is low pressure by application with start to be reduced in lignin and from the cellulose fibre of described living beings hemicellulose between bonding and the moisture of the living beings chip received described in improving, and the steam then by application with more high pressure is heated any gas of described living beings inside existence and fluid and pressurizes, the described overall structure of the living beings in chip formation received described in internal division with the reduction of blood pressure in high-speed of the close-burning described living beings via the moisture and reduction with raising, the described living beings being wherein produced as the fine particulate form of described humidity from the steam blasting unit of described two sections or more sections have and are less than 70 micron thickness and the fine particulate form being less than the average-size of 500 microns long, and the living beings fine grained of those humidities produced is fed to the feeding district of described biomass gasifying furnace subsequently, and

Described living beings fine grained is reacted, described living beings fine grained has the granular size of reduction and the overall surface area increased owing to the division by described two sections of the described steam blasting unit in described biomass gasifying furnace or more sections compared to the described living beings in chip formation being used as raw material received, wherein deposit in the case of steam in described biomass gasifying furnace, the described particle of the described living beings produced by described steam blasting unit reacts to produce at least synthesis gas components with quick bio matter gasification reaction, comprise hydrogen (H2) and carbon monoxide (CO), wherein said steam blasting unit and described biomass gasifying furnace are parts for described integrated equipment.

13. methods for described integrated equipment according to claim 12, wherein said two sections or more sections comprise hot water processing section and steam blasting section, the low-pressure steam soaked into moisture is applied in the container of the described living beings in chip formation of accommodation by wherein said hot water processing section under the pressure of about normal pressure PSI under higher than 60 degrees Celsius but lower than the high temperature of 145 degrees Celsius, thus start to decompose, the living beings in chip formation received described in hydration process also softens, the described chip of wherein said living beings stops considerable 10 to 15 minutes to soak into moisture in described hot water processing section, and wherein said hot water processing section will be fed to described steam blasting section through softening and that moisture improves living beings chip, described steam blasting section under 160 pressure to 450PSI and temperature maintain between 160 to 270 DEG C.

14. methods for described integrated equipment according to claim 12, it comprises further:

Under 160 to 450PSI through the described living beings of pressurization to be left by outlet opening described steam blasting section to maintain lower than pressure in described steam blasting section 1/3rd pressure under purge pipeline before mechanically stir the described living beings in described steam blasting section so that in the described living beings of internal division through pressurizeing under 160 to 450PSI, the described mechanical agitation wherein in described refining section is configured to make gained living beings of a granular form have the more consistent size distribution of the average-size of described biological particles with the one or more blades in refining section.

15. methods for described integrated equipment according to claim 13, wherein after described hot water processing section, described in chip formation through softening living beings through 1) extruding and 2) any combination of compressing, it is then fed to conveyer system, described living beings move in described steam blasting section by described system, wherein in described conveyer system, described living beings prevent from the back-pressure of the blowback of the high steam existed in comfortable described steam blasting section to affect described hot water processing section.

16. methods for described integrated equipment according to claim 12, described two sections of wherein said steam blasting unit or more sections comprise hot water processing section and steam blasting section, steam is applied to described living beings by wherein said hot water processing section, use described steam be detained 8 to 20 minutes time chien shih its higher than 60 DEG C, so that softening and raising moisture, and then described living beings are delivered to the described steam blasting section of described living beings with the living beings in chip formation described in internal division, wherein said living beings are exposed to the sufficient time section continuing 3 to 15 minutes in high temperature and high pressure steam living beings between 160 to 450 pounds/square inch, high steam is formed with other inside, porous zone in the described overall structure of biological material described in the cellulose fiber peacekeeping of part hollow, and then make the pressure in the exit in described steam blasting section decline fast, method be by the described overall structure of the described living beings between 160 to 450 pounds/square inch is stretched into be less than described 160 to 450 pounds/square inch 1/3rd decompression under pipe in cause Internal explosions, described living beings are split into living beings fine particle in inside by it.

17. methods for described integrated equipment according to claim 14, wherein said living beings pass through the fine particulate form using the described outlet opening explosion of two or more pressure drops a series of through controlling of different-diameter section instead of the described steam blasting section of single continuous print diameter pressure drop to become described humidity, and wherein once described living beings explosion becomes the fine particulate form of described humidity, described produced biological particles is owing to steam flash and be discharged as steam and lose the percentage of described moisture, the fine grain moisture of wherein said living beings becomes dry further by flash dryer, fine grain for living beings described moisture is reduced to by weight lower than 20% by this.

18. methods for described integrated equipment according to claim 14, wherein said the produced living beings fine grained with the moisture of reduction comprises into cracked, tear, that tear up and any combination and have and be less than 50 micron thickness and the cellulose fibre being less than the average-size of 200 microns long, wherein said produced living beings fine grained is fed to described biomass gasifying furnace for the described quick bio matter gasification reaction in the reactor of described biomass gasifying furnace to downstream, because they form higher surface-to-volume ratio compared to the described living beings in chip formation received for the living beings of identical amount, this allows higher heat and quality to be delivered to more rapid thermolysis and the gasification of all molecules in described biological material and described living beings.

19. methods for described integrated equipment according to claim 12, it comprises further:

Collect in the discharge exit of described steam blasting unit and be reduced to compared with small particle size and described living beings in slurry form and be fed to water separative element, wherein in hydrocyclone unit, remove water from the described living beings in fine particulate form and the described living beings in fine particulate form are fed to flash dryer to be reduced to the described moisture of the described living beings in fine particulate form by weight lower than 20% further lower than the moisture of the described reduction of 40% by weight.

20. methods according to claim 19, wherein after described hot water processing section, described in chip formation through softening living beings through 1) extruding and 2) and compress be anyly combined into plug form, it is then fed to continous way conveying worm system, the described living beings in plug form move in described steam blasting section by described system, wherein in described continous way conveying worm system, the described living beings in described plug form prevent from the back-pressure of the blowback of the high steam existed in comfortable described steam blasting section to affect described hot water processing section, and

The described synthesis gas components comprising hydrogen (H2) and carbon monoxide (CO) wherein from described biomass gasifying furnace is fed to downstream methanol synthesis reactor to form methyl alcohol, and described reactor is also a part for described integrated equipment.