CN101880552A - Gasification device and method for preparing hydrogen-rich synthetic gas from biomass - Google Patents
Gasification device and method for preparing hydrogen-rich synthetic gas from biomass Download PDFInfo
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Abstract
The invention provides a gasification device and a gasification method for preparing hydrogen-rich synthetic gas from biomass. The device comprises a biomass feeder, a mixer, a pyrolysis chamber, a gasification chamber, a gasified gas separator, a combustion chamber, a flue gas separator, a bin and a butterfly valve. In the method, the biomass gasifying process is divided into three parts, namely biomass pyrolysis, semicoke gasification and heat carrier circulation. Through the method and the device, the synthetic gas with the tar content less than 200mg/Nm<3> and the H2/CO ratio more than 1.1 can be obtained, and the energy utilization rate and the process economy are obviously improved.
Description
Technical field
The present invention relates to a kind of biomass gasification technology field, relate in particular to a kind of gasification installation and method of utilizing biomass to produce hydrogen-rich synthetic gas.
Technical background
Physics and chemical process that gasifying biomass takes place mainly comprise biomass drying, pyrolysis, gasification and gas-phase reaction etc., and above-mentioned pyrolysis, gasification all can produce tar.During 400 ℃ of pyrolysis reaction temperature, generate sugar, aldehyde, acid compounds behind the biomass devolatilization, maleic, cyclopentadiene are the main precursors of formation tar; Along with temperature of reaction rises, these precursors generate phenolic compound through taking off reactions such as H, polymerization; When further raising temperature of reaction to 900 ℃, tar is mainly replaced polycyclic aromatic hydrocarbons and is formed by polycyclic aromatic hydrocarbons, alkyl.According to the temperature variant characteristics of tar component, Milne and Evans are divided into three classes with biomass coke tar: with sugar, aldehyde is the first kind tar (primary tar) of representative; With the phenols is the second class tar (secondary tar) of representative; Replacing polycyclic aromatic hydrocarbons with polycyclic aromatic hydrocarbons, alkyl is the 3rd class tar (tertiary tar) of representative.
Studies show that, adopt updraft type fixed bed, fluidized-bed, the thick product gas of downdraft fixed bed gasification gained tar content to be roughly 100g/Nm
3, 10g/Nm
3, 1g/Nm
3There are dependency in the multi-form reactor and the main component of tar, the main first kind tar that generates of updraft type gasification, and the main component that the downdraft gasification produces tar is the 3rd class tar, fluidized-bed gasification gained tar is based on second class, the 3rd class tar.
The too high harm of tar content can be summarized as in the thick product gas: 1) increase gas sweetening intractability and complexity; 2) but tar light oil such as phenol are dissolved in the washing water polluted-water, can form crystallization as naphthalene and stop up valve and generating set, heavy tar can stop up the oil engine side cooler in that condensation takes place below 350 ℃; 3) corrodible oil engine of the contained acidic substance of tar or internal combustion turbine cylinder; 4) reduce system's gasification efficiency and efficiency of energy utilization.
Therefore could use after biomass gasified gas must purify, tar removes technology and can be divided into and remove (as catalytic pyrolysis in oxicracking, thermo-cracking, the stove) in the stove and stove is removed (as catalytic pyrolysis, cloth bag filtration outside the stove, wash, electrostatic capture) dual mode outward.Typical technology can be divided into following three kinds: 1) gasification+rhombspar is defended the catalysis of the main bed of bed+Ni base; 2) high temperature pyrolysis; 3) charcoal catalytic pyrolysis.Handling tar content 2g/Nm based on Ni is catalyst based
3Thick product gas the time catalytic activity fact that sharply descends, Spain Univ Zaragoza proposes in the stove, stove removes process combined outward: increased the three-wave-length gasification that rhombspar is defended bed before the catalyst based main bed of Ni, do like this and both can avoid the catalyst based inactivation of Ni too fast, can obtain tar content again and be lower than 200mg/Nm
3The synthetic gas than high-cleanness, high.Second kind of technology is that Thailand Asia technical institute proposes, and produces high temperature with thermo-cracking tar by introduce secondary air to the vapourizing furnace reduction zone, thereby reaches the purpose that reduces tar.The third is fixed-bed pyrolysis-gasification two-stage gasifier that Technical University Of Denmark proposes, it make biomass not gasification char go out the interruption-forming charcoal bed at vapourizing furnace, utilize the reductive action catalytic pyrolysis tar of high temperature charcoal bed, the two kinds of technologies in back belong to a kind of multi-stage type gasification together, by gasification is carried out pyrolysis, gasification reaction in different reactor or same reactor different zones, can be at different reaction zone optimal control reaction conditionss, make each conversion process and operational condition reach optimum state, thereby improve gasification efficiency and aerogenesis quality with the reduction tar content.
There is tangible weakness respectively in above-mentioned three kinds of technologies, and Pintsch process arts demand combustion parts combustible gas makes reactor reach 1000 ℃ high temperature, thereby sacrifice the calorific value of gasification gas; The two-part gasifying process needs a large amount of thermals source to supply with pyrolysis chamber's pyrolysis, and there is the shortcoming of amplifying difficulty in fixed bed; Though three-wave-length technology can obtain the higher gas of cleanliness factor, required cost is too high, and economy is very poor.
Gasification technology has been widely used in other occasions that comprise generating so far, as be used for biomass-based liquid fuel technology, biomass-based fuel cell technologies etc., these technology form to propose higher requirement to gasification gas, the synthetic gas H that is produced as the conventional air gasification technology
2/ CO ratio has only between the 0.25-0.50, even if adopt O
2-steam gasification also can only reach 0.60-0.87, yet requires the H of unstripped gas when being used for Fischer-Tropsch synthetic fluid hydrocarbon fuel or dme
2The ratio of/CO maintains between the 1.1-2.0; Meanwhile, for reducing the running cost of downstream tar removing process, the tar content in the thick product gas is maintained 200mg/Nm
3Below be one of reliable measure that improves the gasification technology economy, therefore must seek other feasibility height, broad-spectrum novel process.
Summary of the invention
For overcoming the shortcoming of existing biomass gasification technology, the invention provides gasification installation and method that a kind of biomass prepare the low tar hydrogen-rich synthetic gas.
For achieving the above object, the present invention has taked following technical scheme:
Gasification installation of the present invention is a kind of biomass circulating fluid bed gasifying apparatus, and this device comprises: biomass feeder, mixing tank, pyrolysis chamber, vaporizer, gasification gas separating device, revert pipe, auxiliary fuel feeder, combustion chamber, smoke separator, feed bin, dish valve.According to biomass feed and solid particulate circulating path, these component locations and mode of connection are followed successively by: the biomass feeder is connected with mixing tank by filling tube, the mixing tank upper end connects the dish valve, the lower end connects the pyrolysis chamber, pyrolysis chamber's outlet is provided with the convergent conical tube, most of cone is inserted the vaporizer right side, and cone section start and cone end are provided with air/O respectively
2With the water vapour intake, vaporizer is isolated the left and right sides that becomes bottom UNICOM through central dividing plate, and bottom, the vaporizer left and right sides all is provided with air/O
2Intake, bottom, vaporizer right side also is provided with slag-drip opening, vaporizer left side top introduction pipe connects the upside of gasification gas separating device, middle and upper part, vaporizer left side is connected with the bottom, combustion chamber by revert pipe, gasification gas separating device bottom is provided with the solid particulate feed bin, and stopping valve is installed in the feed bin bottom is connected with the bottom, combustion chamber with the returning charge at intermittence to the combustion chamber, auxiliary fuel charging opening and primary air intake being set bottom the combustion chamber, the middle and upper part, combustion chamber is provided with the secondary air intake.The top of combustion chamber outlet connects smoke separator, and smoke separator top is provided with the fume emission mouth, and the smoke separator bottom is provided with feed bin, and the feed bin bottom connects the dish valve.
Described dish valve is by dish valve outlet port pipe and mixing tank UNICOM, and this outlet pipe inserts the mixing tank cavity, and insertion portion length is 1-1.5 times of the outlet pipe internal diameter, and is inside collapsed shape, can play the effect of water conservancy diversion solid thermal carriers.
Described mixing tank is made up of the cylinder barrel shaped cavity on top and the conical cavity of bottom, the ratio of both height is 3-4: 1, the upper end of this cavity is connected with the outlet pipe of dish valve, lower end and pyrolysis chamber link, at axial line arc conical surface particle deflection cone is installed, deflection cone supports by supporting tube, between dish valve outlet port pipe and deflection cone, filling tube is set, the cambered surface radian of the deflection cone arc conical surface is 45-60 °, filling tube and mixing tank axle center line direction are 15-30 ° of angle, and the projection of filling tube outlet port will all be positioned on the deflection cone and the close mixing tank axle center of palpus line one side.The more close in the axial direction dish valve outlet port of filling tube exit end pipe pipe end, and away from the deflection cone cambered surface.
Described pyrolysis chamber is a cylindrical tube, the pyrolysis chamber is arranged alternately the half elliptic baffle plate that is 45-60 ° of angle and tilts upward with axial line along about the axial line both sides, described baffle plate elliptical center place is fixed on the barrier support, the baffle plate upper limb is near pyrolysis chamber's right cylinder inwall but do not come in contact, the barrier support placement location overlaps with pyrolysis chamber's axial line, according to pyrolysis chamber's internal diameter and biological particles size, each baffle spacing 0.3-0.6m, baffle plate number 5-10 piece.The exit, pyrolysis chamber carries out the transition to the slightly little cylindrical tube of diameter by back taper reducing cone, and this cylindrical tube inserts the vaporizer right side, inserts length and is about between the 1/3-1/2 of vaporizer right side height, and 4 air/O are set on the cross section at cone upper limb place
2Intake, small diameter cylinders shape cylindrical shell lower edge is provided with 4 water vapour intakes, described air/O on the cross section
2Intake, water vapour intake are symmetrical distribution at four semi-cardinal pointss that lay respectively at cross section of living in.
Described vaporizer be a bottom UNICOM, top by the isolated cuboid bubbling reactor of vaporizer dividing plate, i.e. vaporizer left side, right side two portions.Dividing plate is positioned at the middle of rectangular parallelepiped vaporizer, and the dividing plate height is the 2/3-4/5 of vaporizer right side height.The right side vaporizer links to each other with pyrolysis chamber's outlet, and vaporizer bottom in right side is provided with 1 slag-drip opening and 4 air/O
2Intake.Vaporizer top, described left side connects the gasification gas separating device, and the about vaporizer height in the left side of left side vaporizer 4/5 place is provided with the solid particulate outlet, is connected with the bottom, combustion chamber by revert pipe, and vaporizer bottom in left side also is provided with 1 air/O
2Intake, the vaporized chemical of this inlet has the effect of fluidization air concurrently.
Described gasification gas separating device bottom connects stopping valve, and stopping valve connects outlet pipe and is connected with the bottom, combustion chamber, and gasification gas separating device top is provided with syngas outlet.
Bottom, described combustion chamber is provided with auxiliary fuel charging opening and primary air intake, and the about 1/2-2/3 in middle and upper part, combustion chamber highly locates to be provided with the secondary air intake.The top of combustion chamber outlet connects smoke separator.
The method that biomass of the present invention prepare low tar, hydrogen-rich synthetic gas is the circulating fluidized bed gasifying process, and its process program is as follows: divide the gasification of form biomass pyrolysis, semicoke, thermal barrier three parts that circulate with traditional CFB biomass gasification process.Biomass are mixed with sorbent material after biomass feeder feed moves to mixing tank by filling tube, and the mixing tank place with carry out the heat transmission rapidly after thermal cyclic carrier, flying dust mix; Solid particulates such as biomass, thermal barrier and sorbent material quicken to enter the pyrolysis chamber under action of gravity, biomass and thermal barrier, sorbent material carry out the catalytic pyrolysis of biomass reaction fully to separate out fugitive constituent when mixing in that pyrolytic reaction is indoor; Cone upper limb place's introducing air or O at pyrolysis chamber's outlet section
2, feed the semicoke that water vapour obtains with pre-gasified bio-matter pyrolysis in the exit, pyrolysis chamber; Respectively in vaporizer left side, the vaporized chemical intake bubbling air or the O on right side
2With the semicoke second gasification, and irregularly discharge slag by the slag-drip opening on vaporizer right side; Standby behind gasification gas separating device isolation of purified from vaporizer left side top vent gas oxidizing gases, Qi Hua semicoke, thermal cyclic carrier, absorbent particles do not move to the bottom, combustion chamber through revert pipe; Add auxiliary fuel in the bottom, combustion chamber, and introduce primary air with semicoke, auxiliary fuel oxidation, but the high temperature heating cycle thermal barrier and the calcination and regeneration sorbent material that produce, described secondary air is the after-flame carbon residue further, and combustion product gases discharges behind cyclonic separator; Sorbent material, flying dust after thermal barrier, the regeneration carries the combustion chamber and absorbs heat and participate in the next round circulation and for pyrolytic reaction provides heat, tail gas is to be rich in CO through feed bin, butterfly valve
2Combustion product gases.
The effect of the baffle arrangement that the pyrolysis chamber is provided with is: after solid particulates such as biomass, thermal barrier and sorbent material quicken to enter the pyrolysis chamber under action of gravity, through pyrolysis chamber's baffle plate stop and to be decelerated to convergence static, landing downwards on the pyrolysis chamber's baffle plate that tilts subsequently, again be accelerated under action of gravity in the process of landing, experience acceleration-deceleration working cycle repeatedly is to increase the residence time of above-mentioned solid particulate in the pyrolysis chamber.
Before beginning, gasification reaction can feed primary air and secondary air, and to combustion chamber input auxiliary fuel, throw in the mixture of thermal barrier and sorbent material after about 0.5-1 hour, thermal barrier and sorbent material drop into total mass to be decided on combustion chamber fluidisation ability and biomass feeding quantity, can keep between the circulation ratio 10-25 usually.Described slag-drip opening carries out irregular deslagging can make that thermal barrier and sorbent material total mass tail off in the stove, so biomass are answered the continuous supplementation sorbent material when reinforced.The absorbent particles that is used for catalytic cracking of tar and solid carbon can mix the back charging with biomass, also can adopt independently feeding machine charging.
Gu described sorbent material is inhaled with solid particulate circulation catalytic pyrolysis-carbon-calcine sequential reaction takes place: 1) in pyrolysis chamber's catalyse pyrolysis biomass; 2) participate in reaction of catalytic pyrolysis tar and solid carbon reaction at vaporizer; 3) after turning back to the combustion chamber, take place and high-temperature calcination reaction, discharge CO when recovering porous surface
2
Described pyrolysis chamber outlet section gas, solid fluidal texture are the moving-beds that slowly moves downward, and semicoke gasifies in the process that moves down in advance, and the solid particulate translational speed depends on the vaporized chemical gas flow size that introduce the vaporizer bottom; The gas of described vaporizer, solid fluidal texture are concentrated phase bubbling beds.The pyrolysis gas that contains tar and precursor thereof passes the moving-bed-bubbling bed structure of semicoke, sorbent material, thermal barrier composition, and the second gasification reaction takes place under the vaporized chemical effect semicoke; Tar component is become micro-molecular gas by catalytic pyrolysiss such as red-hot semicoke, adsorbent activity component, flying dusts; Sorbent material absorbs the CO that gasification generates
2, because of having reduced the CO in the reactor
2Dividing potential drop can promote water-gas transformationreation to generating H
2Direction moves, thereby can obtain high H
2The gasification gas of content, low tar content.
Described sorbent material can be a kind of in Wingdale, rhombspar or the peridotites, and described vaporized chemical is air, O
2, in the water vapour one or both.Described thermal barrier can be quartz sand or river sand, the mass ratio about 30% of sorbent material and thermal barrier, and the sorbent material continuous-feeding accounts for the 3-10% of total feeding coal.
Described gasification reaction equivalence ratio 0.20-0.35, water vapour feeding amount is kept water vapour/biomass 0.3-1.0.
The pyrolytic reaction actuator temperature is 400-900 ℃, and preferred 500-750 ℃, the residence time, the gasifying reactor temperature of reaction was 600-1000 ℃ greater than 1s, preferred 700-850 ℃, and combustion chamber temperature of reaction 800-1200 ℃, preferred 850-1000 ℃.
The present invention can obtain tar content and be lower than 200mg/Nm
3, H
2/ CO compares the synthetic gas greater than 1.1, is characterized in:
Behind biomass/sorbent material feed in short mix such as mixing tank place and thermal barrier, flying dusts, heat up and fast pyrogenation rapidly;
2. baffle plate increase solid back-mixing is set in the pyrolysis chamber is beneficial to further pyrolysis;
3. pyrolysis chamber's outlet is that the vaporizer inlet adopts the reducing form, and dwindles place and expansion place difference introducing air/O at reactor volume
2And water vapour, make full use of the gasification reaction characteristics, help reaction of biomass oxygen-rich gasification and steam gasification reversible reaction and move to the positive reaction direction;
4. the adsorbent activity component is caught CO at vaporizer
2,, obtain hydrogen-rich gas to promote steam reforming reaction;
Unreacted semicoke and auxiliary fuel in combustion chambers burn with the heat hot carrier, and the calcining sorbent material obtain activeconstituents and recover the porous active surface;
6. but sorbent material catalysis biomass pyrolytic reaction; But semicoke, sorbent material catalytic tar scission reaction.
Compared with prior art, the present invention controls biomass pyrolytic, coke/sorbent material catalytic pyrolysis tar, coke gasification and tar thermo-cracking, process combustion step by step in CFB different zones realization gasification reaction process, has following advantage:
1) separate biomass pyrolytic is relative with gasification, realize the optimum control of various process: biomass pyrolysis process heats up rapidly, can effectively avoid the polymerization of pyrolytic process tar molecule to grow up, and the control pyrolytical condition can be realized that tar is directed and overflow; According to the phasic characteristics of gasification, utilize the pyrolysis char of biomass self to suppress the tar generation, realize the semicoke catalyzed conversion of tar and the orientation regulation and control of thermo-cracking and gaseous fraction;
2) heat of biomass pyrolytic needs is provided by thermal cyclic carrier, and pyrolysis chamber, vaporizer conduct heat, mass transfer condition optimization can realize that uniform temperature distributes, and significantly improves the capacity usage ratio of system;
3) sorbent material both can be played the part of the thermal barrier role in whole technology, can effectively promote biomass gasification reaction again: reduce gas phase CO by the solid carbon reaction of vaporizer adsorbent activity component
2Concentration effectively promotes water-gas transformationreation to obtain hydrogen-rich synthetic gas; Promote the steam gasification reaction by the solid carbon reaction of adsorbent activity component and water-gas transformationreation exothermic effect.The gasification gas H that obtains
2/ CO realizes adsorbent reactivation greater than 1.1 by the combustion chamber calcination reaction, recovers active porous surface, and tail gas is rich in CO
2Be easy to capture;
4) adopt sorbent material cheap and easy to get to avoid complicated downstream tar to remove equipment and technology, and do not sacrifice gas heating value, do not need gasification gas H
2/ CO mol ratio is carried out modified, has improved the economy of biomass gasification process.
Description of drawings
Fig. 1 is that the ciculation fluidized bed gasifying apparatus of the embodiment of the invention is always schemed.
Fig. 2 is an embodiment of the invention internal mixer structural representation.
Fig. 3 is an embodiment of the invention pyrolysis chamber internal structure synoptic diagram.
Fig. 4 is embodiment of the invention vaporizer internal structure and cloth wind, slag-drip opening structural representation.
Description of reference numerals: 1-biomass feeder, 2-mixing tank, 3-pyrolysis chamber, 4-vaporizer, the 5-gas separating device that gasifies, the 6-revert pipe, the 7-grid distributor, 8-combustion chamber, 9-smoke separator, the 10-feed bin, 11-dish valve, 12-dish valve outlet port pipe, 13-biomass filling tube, 14-deflection cone, 15-deflection cone pillar stiffener, 16-pyrolysis chamber baffle plate, 17-barrier support, 18-vaporizer dividing plate.
Embodiment
The present invention will be further described below in conjunction with the drawings and specific embodiments.
As shown in Figure 1, apparatus of the present invention structure is: biomass feeder 1 is connected with mixing tank 2 by biomass filling tube 13, mixing tank 2 upper ends connect dish valve 11, the lower end connects pyrolysis chamber 3, pyrolysis chamber's 3 outlets are provided with the convergent conical tube, most of cone is inserted vaporizer 4 right sides, and setting of cone section start and cone end are provided with air/O respectively
2With the water vapour intake, vaporizer 4 is isolated the left and right sides that becomes bottom UNICOM through central dividing plate, and bottom, vaporizer 4 left and right sides all is provided with air/O
2Intake, bottom, vaporizer 4 right sides also is provided with slag-drip opening, vaporizer 4 left side top introduction pipes connect the upside of gasification gas separating device 5, middle and lower part, vaporizer 4 left side is connected with 8 bottoms, combustion chamber by revert pipe 6, gasification gas separating device 5 bottoms are provided with the solid particulate feed bin, and stopping valve is installed in the feed bin bottom bottom the combustion chamber, is connected with the returning charge at intermittence to the combustion chamber 8,8 bottoms, combustion chamber are provided with auxiliary fuel charging opening and primary air intake, and 8 middle and upper parts, combustion chamber are provided with the secondary air intake.Combustion chamber 8 top exits connect smoke separator 9, and smoke separator 9 tops are provided with the fume emission mouth, and smoke separator 9 bottoms are provided with feed bin 10, and feed bin 10 bottoms connect dish valve 11.
Described dish valve 11 is by dish valve outlet port pipe 12 and mixing tank 2 UNICOMs, and this outlet pipe inserts mixing tank 2 cavitys, and insertion portion length is 1-1.5 times of the outlet pipe internal diameter, and is inside collapsed shape, can play the effect of water conservancy diversion solid thermal carriers.
As shown in Figure 2, described mixing tank 2 is made up of the cylinder barrel shaped cavity on top and the conical cavity of bottom, the ratio of both height is 3-4: 1, the upper end of this cavity is connected with dish valve outlet port pipe 12, lower end and pyrolysis chamber 3 link, at axial line arc conical surface particle deflection cone 14 is installed, deflection cone 14 supports by deflection cone pillar stiffener 15, the cambered surface radian of this arc conical surface is 45-60 °, between dish valve outlet port pipe 12 and deflection cone 14, biomass filling tube 13 is set, biomass filling tube 13 is 15-30 ° of angle with mixing tank 2 direction of axis line, and the projection of biomass filling tube 13 outlet ports will all be positioned on the deflection cone 14 and need near mixing tank 2 axial lines one side.The more close in the axial direction dish valve outlet port of biomass filling tube 13 exit end pipe 12 pipe ends, and away from deflection cone 14 cambered surfaces.
As shown in Figure 3, described pyrolysis chamber 3 is a cylindrical tube, pyrolysis chamber 3 is arranged alternately the half elliptic baffle plate 16 that is 45-60 ° of angle and tilts upward with axial line along about the axial line both sides, described baffle plate 16 elliptical center places are fixed on the barrier support 17, baffle plate 16 upper limbs are near pyrolysis chamber's right cylinder inwall but do not come in contact, barrier support 17 placement locations overlap with pyrolysis chamber's axial line, according to pyrolysis chamber's 3 internal diameters and biological particles size, each baffle spacing 0.3-0.6m, baffle plate number 5-10 piece.3 exits, pyrolysis chamber carry out the transition to the slightly little cylindrical tube of diameter by back taper reducing cone, and this cylindrical tube inserts vaporizer 4 right sides, insert length and are about between the 1/3-1/2 of vaporizer right side height.As shown in Figure 4,4 air/O are set on the cross section at cone upper limb place
2Intake, small diameter cylinders shape cylindrical shell lower edge is provided with 4 water vapour intakes, described air/O on the cross section
2Intake, water vapour intake are symmetrical distribution at four semi-cardinal pointss that lay respectively at cross section of living in.
Described vaporizer 4 be a bottom UNICOM, top by the isolated cuboid bubbling reactor of vaporizer dividing plate, i.e. vaporizer left side, right side two portions.Dividing plate is positioned at the middle of rectangular parallelepiped vaporizer 4, and the dividing plate height is the 2/3-4/5 of vaporizer right side height.The right side vaporizer links to each other with pyrolysis chamber's outlet, and vaporizer bottom in right side is provided with 1 slag-drip opening and 1 air/O
2Intake.Vaporizer top, described left side connects the gasification gas separating device, and the about vaporizer height in the left side of left side vaporizer 4/5 place is provided with the solid particulate outlet, is connected with 8 bottoms, combustion chamber by revert pipe 6, and vaporizer bottom in left side also is provided with 1 air/O
2Intake, this vaporized chemical has the effect of fluidization air concurrently.
Described gasification gas separating device 5 bottoms connect stopping valve, stopping valve connect outlet pipe and with at the bottom of the combustion chamber 8 ones be connected, gasification gas separating device 5 tops are provided with syngas outlet.
8 bottoms, described combustion chamber are provided with auxiliary fuel charging opening and primary air intake, and the about 1/2-2/3 in 8 middle and upper parts, combustion chamber highly locates to be provided with the secondary air intake.Combustion chamber 8 top exits connect smoke separator 9.
Low tar hydrogen-rich synthetic gas technology is produced in one one kinds of wood chip circulating fluidized bed gasifications of embodiment
Use device shown in Figure 1, get the wood raw material of wood-working factory, the technical analysis of wood chip and ultimate analysis are shown in subordinate list 1, wood chip and sorbent material are delivered to mixing tank 2 through biomass feeder 1 by biomass filling tube 13 by 95: 5 mixed, with temperature be 850 ℃ thermal barrier, sorbent material (thermal barrier is 7: 3 with the adsorbent mass ratio) is mixed heat transfer rapidly, change circulation ratio by the aperture of adjusting dish valve 11, wood chip is heated to about 600 ℃, wood chip subsequently, thermal barrier, sorbent material relies on the effect of gravity to quicken to enter pyrolysis chamber 3, through pyrolysis chamber's baffle plate 16 stop and to be decelerated to convergence static, experience the working cycle of continuous acceleration-deceleration, increase the residence time of wood chip in pyrolysis chamber 3 fully to separate out fugitive constituent.The semicoke that obtains after pyrolysis finishes, fugitive constituent move to 3 exits, pyrolysis chamber with thermal barrier, sorbent material etc., and introduce O at gasification agent inlet this moment
2, back taper throat structure has herein dwindled reaction volume, can promote volume to reduce reaction as C and O
2, CO and O
2Between gasification reaction, feed water vapour, O at the gasification agent inlet in reducing section exit
2Introducing amount control equivalence ratio 0.15, water vapour/biomass mass ratio is 0.4.
Described sorbent material is selected from Wingdale, rhombspar or the peridotites a kind of, and described vaporized chemical is selected from air, O
2, in the water vapour one or both, described thermal barrier is quartz sand or river sand; The mass ratio about 30% of sorbent material and thermal barrier, the sorbent material continuous-feeding accounts for the 3-10% of total feeding coal.
Ratio in vaporizer 4 left and right sides bottoms in 4: 6 or 5: 5 feeds O respectively
2, the O of this two place
2Total introducing amount control equivalence ratio is 0.11.Sorbent material, semicoke continue herein catalytic pyrolysis tar, simultaneously adsorbents adsorb CO take place
2, the reaction of semicoke oxygen enrichment-steam gasification.750 ℃ of gasification reaction temperature, gaseous products is drawn after gasification gas separating device 5 separates standby by vaporizer 4 left side top.Solid phase particles such as sorbent material, thermal barrier, flying dust, the intact semicoke of unreacted run to 8 bottoms, combustion chamber through revert pipe 6.
With the auxiliary fuel feed in the combustion chamber 8 bottoms, and burn with so far unreacted semicoke of circulation, liberated heat is with heating cycle thermal barrier and sorbent material, and the high-temperature calcination sorbent material, discharges CO
2The time recover the porous catalytic surface, auxiliary fuel can be coal or biomass, its feeding quantity is decided on furnace temperature, combustion chamber concentrated phase area temperature remains on 900 ℃.8 tops, combustion chamber feed secondary air with further after-flame carbon residue, and combustion product gases obtains thermal barrier after smoke separator 9 separates and reproducing adsorbent continues to participate in the circulation of next round, and is rich in CO
2The flue gas of gas discharges by tail gas funnel.Flue gas can be used to dry biomass fuel, and making reinforced preceding biomass water content is about 10%.
In this embodiment, the gasification gas main component of acquisition is hydrogen, methane, carbon monoxide, carbonic acid gas, ethane, ethene, acetylene, propane, propylene, propine etc.By analysis, the main composition and the physical property of gasification gas are as shown in table 2, and table 2 gives certain gasification process gained gasification gas and forms and physical property simultaneously, by table 2 as seen, adopt gasify H in the synthetic gas that obtains of apparatus of the present invention
2Content is 44.5%, and more traditional gasification mode has improved 86.19%; Tar content is 0.189g/Nm
3, the tradition gasification has reduced by 88.14%; H
2/ CO ratio is 1.36, can be used as the unstripped gas of biomass-based liquid fuel technology.
Technical analysis of table 1 wood chip and ultimate analysis
Table 2 present embodiment and traditional gasification mode gasification result are relatively
Claims (12)
1. one kind prepares the gasification installation of hydrogen-rich synthetic gas by biomass, and it is characterized in that: this device comprises following assembly: biomass feeder, mixing tank, pyrolysis chamber, vaporizer, gasification gas separating device, combustion chamber, smoke separator, feed bin, dish valve; The biomass feeder is connected with mixing tank by filling tube, and the mixing tank upper end connects the dish valve, UNICOM pyrolysis chamber, lower end, and pyrolysis chamber's outlet is provided with the convergent conical tube, and most of cone is inserted the vaporizer right side, and cone section start and cone end are provided with air/O respectively
2With the water vapour intake, vaporizer is isolated the left and right sides that becomes bottom UNICOM through central dividing plate, and bottom, the vaporizer left and right sides all is provided with air/O
2Intake, bottom, vaporizer right side also is provided with slag-drip opening, vaporizer left side top introduction pipe connects the upside of gasification gas separating device, middle and upper part, vaporizer left side is connected with the bottom, combustion chamber by revert pipe, gasification gas separating device bottom is provided with the solid particulate feed bin, and in the feed bin bottom stopping valve is installed and bottom the combustion chamber, is connected with the returning charge at intermittence to the combustion chamber, the bottom, combustion chamber is provided with auxiliary fuel charging opening and primary air intake, the middle and upper part, combustion chamber is provided with the secondary air intake, the top of combustion chamber outlet connects smoke separator, smoke separator top is provided with the fume emission mouth, and the smoke separator bottom is provided with feed bin, and the feed bin bottom connects the dish valve.
2. the gasification installation for preparing hydrogen-rich synthetic gas by biomass as claimed in claim 1, it is characterized in that: described dish valve is by dish valve outlet port pipe and mixing tank UNICOM, this outlet pipe inserts the mixing tank cavity, and insertion portion length is 1-1.5 times of the outlet pipe internal diameter, and is inside collapsed shape.
3. the gasification installation for preparing hydrogen-rich synthetic gas by biomass as claimed in claim 1 or 2, it is characterized in that: described mixing tank is made up of co-axial top cylinder barrel shaped cavity and lower cone shape cavity, the ratio of both height is 3-4: 1, at the cavity axial line arc conical surface particle deflection cone is installed, deflection cone supports by supporting tube, between the dish valve outlet port pipe of UNICOM's mixing tank upper chamber and deflection cone filling tube is set.
4. the gasification installation for preparing hydrogen-rich synthetic gas by biomass as claimed in claim 3, it is characterized in that: the cambered surface radian of the described deflection cone arc conical surface is 45-60 °, filling tube and mixer chamber body direction of axis line are 15-30 ° of angle, and the projection of filling tube outlet port will all be positioned on the deflection cone and close mixer chamber body axial line one side of palpus.
5. the gasification installation for preparing hydrogen-rich synthetic gas by biomass as claimed in claim 1, it is characterized in that: described pyrolysis chamber is a cylindrical tube, the pyrolysis chamber is arranged alternately the half elliptic baffle plate that is 45-60 ° of angle and tilts upward with axial line along about cylindrical shell axial line both sides, described baffle plate elliptical center place is fixed on the barrier support, the baffle plate upper limb is near pyrolysis chamber's right cylinder inwall but do not come in contact, the barrier support placement location overlaps with pyrolysis chamber's cylindrical shell axial line, the exit, pyrolysis chamber carries out the transition to the slightly little cylindrical tube of diameter by back taper reducing cone, and this cylindrical tube inserts the vaporizer right side.
6. the gasification installation for preparing hydrogen-rich synthetic gas by biomass as claimed in claim 1, it is characterized in that: described vaporizer is that a bottom UNICOM, top are by the isolated cuboid bubbling reactor of vaporizer dividing plate, dividing plate is positioned at the middle of rectangular parallelepiped vaporizer, and the dividing plate height is the 2/3-4/5 of vaporizer right side height; The right side vaporizer links to each other with pyrolysis chamber's outlet, and vaporizer bottom in right side is provided with 1 slag-drip opening and 4 air/O
2Intake, vaporizer top, left side connect the gasification gas separating device, and the about vaporizer height in the left side of left side vaporizer 4/5 place is provided with the solid particulate outlet, are connected with the bottom, combustion chamber by revert pipe, and vaporizer bottom in left side also is provided with 1 air/O
2Intake.
7. the gasification installation for preparing hydrogen-rich synthetic gas by biomass as claimed in claim 1, it is characterized in that: described gasification gas separating device bottom connects stopping valve, stopping valve connects outlet pipe and is connected with the bottom, combustion chamber, and gasification gas separating device top is provided with syngas outlet.
8. as claimed in claim 1ly prepare the gasification installation of hydrogen-rich synthetic gas by biomass, it is characterized in that: bottom, described combustion chamber is provided with auxiliary fuel charging opening and primary air intake, and middle and upper part, combustion chamber 1/2-2/3 highly locates to be provided with the secondary air intake.
One kind use claim 1 device prepare the method for hydrogen-rich synthetic gas by biomass, it is characterized in that: divide form biomass pyrolysis, semicoke gasification, thermal barrier three parts that circulate biomass gasification process; Biomass are mixed with sorbent material after biomass feeder feed moves to mixing tank by filling tube, and the mixing tank place with carry out the heat transmission rapidly after thermal cyclic carrier, flying dust mix; Solid particulates such as biomass, thermal barrier and sorbent material quicken to enter the pyrolysis chamber under action of gravity; When mixing, biomass and thermal barrier, sorbent material carry out the catalytic pyrolysis of biomass reaction fully to separate out fugitive constituent in the pyrolysis chamber; Cone upper limb place's introducing air or O at pyrolysis chamber's outlet section
2, feed the semicoke that water vapour obtains with pre-gasified bio-matter pyrolysis in the exit, pyrolysis chamber; Respectively in vaporizer left side, the vaporized chemical intake bubbling air or the O on right side
2With the semicoke second gasification, and irregularly discharge slag by the slag-drip opening on vaporizer right side; Standby behind gasification gas separating device isolation of purified from vaporizer left side top vent gas oxidizing gases, Qi Hua semicoke, thermal cyclic carrier, absorbent particles do not move to the bottom, combustion chamber through revert pipe; Add auxiliary fuel in the bottom, combustion chamber, and introduce primary air with semicoke, auxiliary fuel oxidation, but the high temperature heating cycle thermal barrier and the calcination and regeneration sorbent material that produce, described secondary air is the after-flame carbon residue further, and combustion product gases discharges behind cyclonic separator; Sorbent material, flying dust after thermal barrier, the regeneration carries the combustion chamber and absorbs heat and participate in the next round circulation and for pyrolytic reaction provides heat, tail gas is to be rich in CO through feed bin, dish valve
2Combustion product gases.
10. biomass as claimed in claim 9 prepare the method for hydrogen-rich synthetic gas, it is characterized in that: after solid particulates such as biomass, thermal barrier and sorbent material quicken to enter the pyrolysis chamber under action of gravity, through pyrolysis chamber's baffle plate stop and to be decelerated to convergence static, landing downwards on the pyrolysis chamber's baffle plate that tilts subsequently, again be accelerated under action of gravity in the process of landing, experience acceleration-deceleration working cycle repeatedly is to increase the residence time of above-mentioned solid particulate in the pyrolysis chamber.
11. biomass as claimed in claim 9 prepare the method for hydrogen-rich synthetic gas, it is characterized in that: before gasification reaction begins, promptly feed primary air and secondary air, and to combustion chamber input auxiliary fuel, throw in the mixture of thermal barrier and sorbent material afterwards, thermal barrier and sorbent material drop into total mass to be decided on combustion chamber fluidisation ability and biomass feeding quantity; Described slag-drip opening carries out irregular deslagging can make that thermal barrier and sorbent material total mass tail off in the stove, so biomass are answered the continuous supplementation sorbent material when reinforced; The absorbent particles that is used for catalytic cracking of tar and solid carbon can mix the back charging with biomass, also can adopt independently feeding machine charging.
12. prepare the method for hydrogen-rich synthetic gas by claim 9 or 11 described biomass, it is characterized in that: described sorbent material is selected from Wingdale, rhombspar or the peridotites a kind of, described thermal barrier is quartz sand or river sand; The mass ratio about 30% of sorbent material and thermal barrier, the sorbent material continuous-feeding accounts for the 3-10% of total feeding coal.
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| CN108707478A (en) * | 2018-06-22 | 2018-10-26 | 华北电力大学 | Multiple stage circulation fluidisation bed solid fuel produces the device and method of hydrogen-rich synthetic gas |
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| CN113322102A (en) * | 2021-05-27 | 2021-08-31 | 江苏大学 | System for preparing hydrogen-rich synthesis gas by biomass staged gasification |
| CN115261079A (en) * | 2022-08-25 | 2022-11-01 | 西安交通大学 | Circulating fluidization device and method for preparing synthesis gas |
| CN115261079B (en) * | 2022-08-25 | 2023-08-15 | 西安交通大学 | Circulating fluidization device and method for preparing synthesis gas |
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