CN100357396C - Method and device for thermolysis preparing liquid fuel from steam explosion stalk fermented residue - Google Patents
Method and device for thermolysis preparing liquid fuel from steam explosion stalk fermented residue Download PDFInfo
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- CN100357396C CN100357396C CNB2005100111043A CN200510011104A CN100357396C CN 100357396 C CN100357396 C CN 100357396C CN B2005100111043 A CNB2005100111043 A CN B2005100111043A CN 200510011104 A CN200510011104 A CN 200510011104A CN 100357396 C CN100357396 C CN 100357396C
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Abstract
The present invention belongs to the technical field of energy source chemical industry, and particularly relates to a method and a device for preparing liquid fuel (biologic oil) which has high quality from steam explosion stalk fermented residue in a fast thermal cracking mode. The method leads the existing thermal cracking reactor to be improved. A rotary screen plate pyrolyzer, a fast separator, a vortex filtering device, a tube array-double wall spray thrower and the like are additionally arranged. After stalk is processed in a steam explosion and fermentation mode, thermal cracking conditions are controlled, the thermal cracking conversion rate of the stalk is enhanced, residue of the stalk is fast and thermally cracked by the rotary screen plate pyrolyzer, and liquid fuel which has the high heating value is obtained. Simultaneously, the acid content of biologic oil is reduced. The present invention provides the method for preparing liquid fuel which has high quality from steam explosion stalk fermented residue, and also provides a device for obtaining biologic oil which has the high liquid yield.
Description
Technical field
The invention belongs to the derived energy chemical technical field, be particularly related to a kind of method and device that utilizes steam explosion stalk fermented residuum fast pyrogenation to prepare high-quality liquid fuel (bio oil), be that stalk passes through that vapour is quick-fried, after the fermentative processing, its residuum obtains the liquid fuel of high heating value through rotation sieve plate pyrolysis reactor fast pyrogenation.
Background technology
The energy and environmental problem have become the focus that the whole world is paid close attention to.Along with industrialized progress, coal and petroleum-based energy consumption cause petering out of resource, bring severe contamination to environment simultaneously, discharge carbonic acid gas in a large number Greenhouse effect are increased the weight of.Biomass are as a kind of important, stable, reproducible substitute energy, because of its sulphur, nitrogen content is low, pollution is little, CO
2Advantage such as zero release, aboundresources is just causing people's extensive concern.
Biomass typically refer to based on terrestrial plant of xylogen, Mierocrystalline cellulose, hemicellulose and other organic matter (as timber, yule logs, stalk) and waterplant etc.China biomass resource total amount is estimated can reach every year more than 6.5 hundred million tons of mark coals, and the stock number of all kinds of agricultural wastes (as stalk etc.) promptly has 3.8 hundred million tons of mark coals every year, and wherein straw, cornstalk, wheat straw account for 31.3%, 27.7%, 16.0% respectively.
The main mode of biomass energy conversion has biochemical method and thermal conversion process two big classes.There is a large amount of fermentation residuums in existing using in the preparing alcohol technologies such as biomass, stalk, is to improve energy transformation efficiency, and these residuums must utilize.By chemical heat method for transformation system bio oil is rational selection.In biomass thermal transformed, fast pyrogenation can obtain 50～70% liquid fuel (timber is 60～70%, and stalk is 50～60%), thereby is subjected to extensive concern both domestic and external.Usually, directly the bio oil calorific value that obtains of pyrolysis biomass is low, acidity is big, oxygen level is high, poor stability (wherein the bio oil calorific value that obtains of pyrolysis stalk is lower, acid content is bigger, moisture more), thereby influences its use.Therefore, how more the good utilisation stalk biomass energy is faced with very big challenge.
In order to obtain high-quality biomass liquid fuel, have more work to concentrate on the catalysis upgrading of catalytic pyrolysis of biomass and bio oil, but effect is all undesirable.Influence the yield of bio oil and the factor that quality has two aspects: be the composition of biomass on the one hand.The biomass composition mainly contains Mierocrystalline cellulose, hemicellulose, xylogen and a small amount of ash content.Mierocrystalline cellulose contains a large amount of hydroxyls; Hemicellulose not only contains hydroxyl, contains carboxyl simultaneously, is the main source of acid in the pyrolysis liquid; The hydroxyl that xylogen contains is less.C/H content height order is xylogen＞Mierocrystalline cellulose＞hemicellulose in these three kinds of main ingredients, how effectively to reduce the acid content of bio oil, improves the key that its calorific value is thermal transition again.For being raw material with timber, the someone adopts pre-treatment to remove wherein hemicellulose, as the dilute acid hydrolysis biomass.For example, US5395455 (1995.7) has announced wood saccharification pre-treatment and fast pyrogenation system liquid bio oil, again to the bio oil system ethanol that ferments; CN1385508 (2002.12) has announced the method for utilizing acid hydrolysis residue system bio oil.Yet the sour water subsequent disposal that these treatment processs produce is difficulty comparatively, and environment is worked the mischief easily, and material through after the acid hydrolysis than thickness, easily agglomerating, increased reinforced difficulty.For being raw material with the stalk, present method also is difficult to produce high-quality biological oil.
Influencing the yield of bio oil and the factor on the other hand of quality is the structure and the condition of reactor.Cracking reactors such as fluidized-bed, circulating fluidized bed and rotation awl are arranged about the many structure of reactor of biomass pyrolytic aspect research at present both at home and abroad.For example, the biomass integrated thermocracking equipment for preparing liquid fuel (CN1390915) that Zhejiang University announces and East China University of Science's announcement prepare the method (CN1385508) of bio oil by the biomass by hydrolyzation residue, its technical scheme all adopts fluidized-bed as pyrolysis reactor.These fluidized bed pyrolysis devices and cyclonic separator, carbon-coating strainer link, and direct then and condenser links.After follow up device compression dehumidifying, return in the burner again.These fluidized bed pyrolysis devices (comprising circulating fluidized bed), though good heat transfer characteristic is arranged, also making pyrolysis secondary steam reaction aggravation because the load volume that uses is big, influences the recovery of pyrolysis steam simultaneously to a certain extent.Holland Twente university has announced the method (US2002117390) of utilizing rotation awl reactor pyrolysis waste material, this reactor does not use carrier gas, the biomass heating rate is fast, but its transformation efficiency influences by structure and operating method and be restricted, and industry is amplified and also restricted.Therefore, analyze existing biomass pyrolysis reactor and have following shortcoming: existing fluidized bed pyrolysis reactor gas residence time is longer, and secondary reaction is serious, has reduced the bio oil quality; Perhaps the particle residence time shorter, pyrolysis is insufficient, the volatile matter transformation efficiency is low.
Summary of the invention
A purpose of the present invention is that existing pyrolysis reactor is improved, rotation sieve plate pyrolyzer, quick disconnector, cyclonic filter device, tubulation-multiple wall spray thrower etc. have been increased, thereby provide a kind of device of thermolysis preparing liquid fuel from steam explosion stalk fermented residue, to overcome the prior art defective.
Another object of the present invention is to utilize device of the present invention, and a kind of method of thermolysis preparing liquid fuel from steam explosion stalk fermented residue is provided.
Design of the present invention is based on that stalk is quick-fried through vapour, fermentation has changed part-structure and composition, by the control pyrolytical condition, improves pyrolysis reactor, improve stalk pyrolysis transformation efficiency, increase the bio oil yield, improve the calorific value of bio oil, reduce the acid content of bio oil.
Cellulosic content accounts for 35～45% in straw biomass (as wheat straw, the cornstalk etc.) plant, and hemicellulose accounts for 20～35%, and xylogen accounts for 15～22%, and ash content accounts for 1～15%.Studies show that the product liquid that each component pyrolysis of biomass obtains is also inequality, the Mierocrystalline cellulose pyrolysis obtains Levoglucosan, glycollic aldehyde and small amount of acid etc.; The hemicellulose pyrolysis obtains products such as furfural, acetate, and the xylogen pyrolysis obtains phenols and tar class product; Ash content is also very big to the pyrolytic influence, can make that pyrolysis product is degraded, and its result directly causes the pyrolysis acid yield to increase.
Research and analyse and show, after stalk biomass being adopted physico-chemical processes such as vapour is quick-fried, fermentation, removed on the one hand wherein half fiber and part Mierocrystalline cellulose and converted it into, also increased content of lignin and C/H ratio in the stalk residuum as byproducts such as xylo-oligosaccharide, ethanol; On the other hand, a small amount of ash content in the stalk is removed in the quick-fried processing of vapour, has also alleviated ash content to the pyrolytic influence degree.Therefore, the pyrolysis of this stalk residuum is expected to obtain than low acid content, the higher bio oil of calorific value.
At the deficiency of existing pyrolysis reactor, be difficult to control as the particle residence time, pyrolysis is insufficient, and the volatile matter transformation efficiency is low; Problems such as perhaps the pyrolytic reaction gas residence time is longer, and secondary reaction is serious are considered the needs that industry is amplified simultaneously, and the present invention adopts rotation sieve plate fast pyrolysis process method, as shown in Figure 1.
Specify the method for thermolysis preparing liquid fuel from steam explosion stalk fermented residue and the operational path and the principle of work of device below in conjunction with accompanying drawing 2～5.
The device of thermolysis preparing liquid fuel from steam explosion stalk fermented residue of the present invention, its parts that are connected by pipeline are formed and are comprised: riser tube burner 1, fume dust remover 2, two-stage screw feeding device 3, hot sand storehouse 4, rotation sieve plate pyrolyzer 5, gas-solid quick disconnector 6, sand coke bin 7, spiral send coke installation 8, cyclone filter 9, tubulation-multiple wall spray thrower 10, deep freezer 11, static trap 12, moisture eliminator 13, compressor 14, gas holder 15, pyrolysis liquid basin 16, oil pump 17, gas meter 18.
The bottom of one riser tube burner 1 has the wind inlet one time, the inside at the riser tube burner 1 on wind inlet top is provided with grid distributor, be positioned on the wall of riser tube burner 1 of grid distributor top and have the burnt import of a sand, and send the outlet of coke installation 8 to be connected by pipeline and spiral; Have the import of pyrolysis dry gas above the burnt import of the sand of riser tube burner 1, the middle part of riser tube burner 1 is provided with the secondary air inlet; Riser tube burner 1 top exit is connected with the first step cyclonic separator top inlet mouth of fume dust remover 2;
The first step cyclonic separator outlet at bottom of one fume dust remover 2 is connected with the top inlet in hot sand storehouse 4, first step cyclonic separator top exit is connected with cyclonic separator top, the second stage inlet mouth of fume dust remover 2, cyclonic separator bottom, the second stage is provided with ash discharging hole, and the top is hot flue gas discharge opening;
One hot sand storehouse, 4 outlet at bottoms add the sand mouth with the top of rotation sieve plate pyrolyzer 5 and are connected, rotation sieve plate pyrolyzer 5 crown centers are equipped with motor 19, and its top is provided with the stalk charging opening and is connected with second stage self-conveyor feed 27 outlets of two-stage screw feeding device 3; Rotation sieve plate pyrolyzer 5 outlet at bottoms are connected with gas-solid quick disconnector 6 top inlet;
The top of one gas-solid quick disconnector 6 is provided with two pneumatic outlets, and is connected with the middle and upper part inlet mouth of cyclone filter 9, and gas-solid quick disconnector 6 outlet at bottoms are connected with the top inlet of sand coke bin 7; Another import that is positioned at sand coke bin 7 upper lateral parts is connected with the outlet at bottom of cyclone filter 9, and sand coke bin 7 outlet at bottoms directly are connected in spiral and send in coke installation 8 imports;
The air outlet, top of one cyclone filter 9 is connected with the pyrolysis steam-in 37 at tubulation-multiple wall spray thrower 10 tops, tubulation-multiple wall spray thrower 10 bottom pyrolysis liquid outlet 40 is connected with liquid inlet, pyrolysis liquid basin 16 top, and the pyrolysis vapour outlet 39 of tubulation-answer wall spray thrower 10 side lower parts is connected with the pyrolysis steam inlet of deep freezer 11 side lower parts; Tubulation-multiple wall spray thrower 10 both sides are distributed with the import and export of cooling medium in tubulation, the multiple wall respectively;
The top of one deep freezer 11 is provided with pneumatic outlet, and is connected with the top inlet mouth of static trap 12, and the outlet of pyrolysis liquid is all established in the bottom of deep freezer 11 and static trap 12, and all the liquid inlet with pyrolysis liquid basin 16 tops is connected; Deep freezer 11 sidepieces are provided with the import and export (not drawing among the figure) of cooling medium;
One static trap, 12 side lower part air outlets are connected with moisture eliminator 13 bottom air inlets, and air outlet, moisture eliminator 13 top links to each other with compressor 14 inlet mouths, and compressor 14 air outlets are connected with gas holder 15 bottom air inlets; Gas holder 15 tops are provided with drain and outer air feed port, and the air outlet of gas holder 15 middle and lower parts links to each other with gas meter 18 inlet mouths, and the air outlet of under meter 18 is connected with the pyrolysis dry gas import of riser tube burner 1 middle and lower part;
One pyrolysis liquid basin, 16 middle and lower parts are provided with the outlet of pyrolysis liquid and are connected with oil pump 17 imports, and oil pump 17 outlets are connected with the circulation pyrolysis liquid inlet at tubulation-multiple wall spray thrower 10 tops; Pyrolysis liquid basin 16 bottoms are provided with the relief outlet of pyrolysis liquid.
Described two-stage screw feeding device 3 is made up of its top stalk feed bin 24 and stalk feed bin bottom first step self-conveyor feed 25, air sealing valve 26 and second stage self-conveyor feed 27, and air sealing valve 26 is between two- stage screw 25 and 27.
Described rotation sieve plate pyrolyzer 5, as shown in Figure 2.The cylindrical shell of rotation sieve plate pyrolyzer 5 is cylindricality, and its bottom is taper.Cylindricality wall top has the sand of adding mouth to link to each other with pyrolysis sand storehouse 4, the pyrolyzer top has the stalk charging opening to link to each other with two-stage screw feeding device 3, the pyrolyzer center of top is equipped with motor 19, motor 19 links to each other with rotating shaft 20 by the sealed attachment part, (10～30cm) are fixed with multiple rotary screen plate 22, starch 21 with a static agitation on every layer of rotation sieve plate 22 according to certain space length in the rotating shaft 20.The pyrolyzer bottom is provided with discharge port, links to each other with the opening for feed of gas-solid quick disconnector 6.
The structure formation of described rotation sieve plate 22 and static agitation slurry 21, as shown in Figure 3.Rotation sieve plate 22 is the garden dish type, is distributed with the sieve aperture 23 that is increased gradually by center diameter to the outer rim direction on the dish.Static agitation slurry 21 is colter shape, connects with rotating shaft 20 loop types.When motor 19 drive rotating shafts 20 and 22 rotations of rotation sieve plate, 21 in static agitation slurry and rotation sieve plate 22 keep the relative movement states.
Described cyclone filter 9, as shown in Figure 1.Its inlet mouth is on wall top, and the lower end, air outlet of center of top links the barrel-shaped metal filter screen in 50～300 purpose gardens, and the cyclone filter bottom is tapered, and the bottom outlet links to each other with sand coke bin 7.
Described tubulation-multiple wall spray thrower 10, as shown in Figure 5.The chuck that the multiple wall of this spray thrower is made up of two-layer cylindrical vessel, the inlet of multiple wall (promptly the wall cooling medium enters the mouth 36 again) is positioned at the right middle and lower part of spray thrower, and the outlet of multiple wall (i.e. wall cooling medium outlet 35 again) is positioned at the upper left quarter of spray thrower.The top of spray thrower is provided with the side entrance 38 of pyrolysis steam-in 37 and circulation pyrolysis liquid.The spray thrower inner shell is equipped with the condensation tubulation 30 of 10～50 coupled in series, forms single passage, and its inlet (being tubulation cooling medium inlet 34) is positioned at the left middle and lower part of spray thrower, and its outlet (being tubulation cooling medium outlet 33) is positioned at the upper right quarter of spray thrower.The top of tubulation is provided with gas-liquid grid distributor 29.It is 30 ° of annular plates (being called solution-air spacer plate 31) that the inner shell of spray thrower and the below that is positioned at condensation tubulation 30 are provided with downward-sloping pitch angle, the below of solution-air spacer plate is solution-air separate chamber 32, be made as two pyrolysis vapour outlets 39 in the top of solution-air separate chamber, the bottom of spray thrower, the bottom of spray thrower or solution-air separate chamber 32 is pyrolysis liquid outlet 40.
The method of thermolysis preparing liquid fuel from steam explosion stalk fermented residue of the present invention:
1. the stalk fermentation residuum (is made up of reinforced spiral 25,27 of two-stage and air sealing valve 26 by two-stage screw feeding device 3 in stalk feed bin 24, quantitatively join on the rotation sieve plate 22 as shown in Figure 4) by rotation sieve plate pyrolyzer 5 tops, and mix with the hot sand that comes self-heating sand storehouse 4, the ratio of mixture of hot sand and stalk material is 8～10: 1 (weight ratio), pyrolysis temperature is 400～700 ℃, and pressure is 0～0.002MPa (gauge pressure).The rotation sieve plate 22 under the drive of motor 19 in, hot sand and stalk material mix rapidly, conduct heat, static agitation slurry 21 plays stirring, blended effect with rotating sieve plate 22 maintenance relative movement, and mixture drops into the enterprising step heat transfer of subordinate's rotation sieve plate, pyrolysis step by step by the sieve aperture 23 of rotation sieve plate 22 like this.Gu the effect of static agitation slurry is the solid-mixing that increases hot sand and pyrolysis material, improves heat transfer efficiency; Solid retention time can be regulated by changing the sieve plate dish number of plies; The rotation of sieve plate dish has reduced the dynamical angle of repose of stalk material, prevents the material bridging, is convenient to material and enters lower floor's sieve plate continuation pyrolysis smoothly.Therefore, can reach the control particle and the residence time of pyrolysis steam in reactor, and make the abundant pyrolysis of stalk material by rotating speed, quantity and the distance between plates of regulating sieve plate.Steam, semicoke and the hot sand that pyrolysis produces is dropped in the gas-solid quick disconnector 6 (seeing application for a patent for invention CN200410080801.X) by the outlet at bottom of rotation sieve plate pyrolyzer 5 together.
2. the gas-solid mixture that is entered by gas-solid quick disconnector 6 tops, sharp separation goes out pyrolysis steam, semicoke and hot sand in separator.The pyrolysis steam that carries a small amount of thin ash enters further cyclonic filter ash disposal in the cyclone filter 9 by the pneumatic outlet of separator upper lateral part.Isolated Jiao of separator and sand are discharged by the bottom and are entered into sand coke bin 7 together.The collected ash of cyclonic filter falls into sand coke bin 7 too by the cyclone filter outlet at bottom.
3. hot sand, the semicoke mixture of storage in sand coke bin 7 enters spiral by its outlet at bottom and send in the coke installation 8, spiral send coke installation 8 that hot sand, semicoke mixture are transported in the riser tube burner 1 by the middle and lower part of riser tube burner 1 to burn, and riser tube burner 1 bottom is provided with gas distribution grid and primary air inlet.Above hot sand, semicoke opening for feed, be provided with the inlet of pyrolysis non-condensable gas, the further heat hot sand of combustion and pyrolysis non-condensable gas.Be provided with the secondary air inlet at the middle part of riser tube 1, replenish air so that semicoke and pyrolysis non-condensable gas fully burn.The temperature of combustion of riser tube is 750～850 ℃, and pressure is 0～0.002MPa (gauge pressure).The hot sand of heating and hot flue gas are through first step cyclonic separator in the fume dust remover 2 at riser tube top, the hot sand that cyclonic separation is come out is stored in the hot sand storehouse 4, and the hot flue gas that carries a small amount of thin ash passes through cyclonic separator dedusting in the second stage in the fume dust remover 2 again, discharged by this cyclonic separator top, the collected thin ash of cyclonic separation is discharged by ash discharging hole.
4. the pyrolysis steam that comes out of cyclone filter 9 tops enters spray thrower by tubulation-multiple wall spray thrower 10 top gas inlet 37, carries the circulation pyrolysis liquid of coming also to enter spray thrower by top circulation pyrolysis liquid inlet 38 by oil pump 17 simultaneously.Pyrolysis steam of being come in by the spray thrower top and circulation pyrolysis liquid direct contact heat-exchanging in gas-liquid grid distributor 29 makes pyrolysis steam rapid condensation, and with pyrolysis steam and be advanced into the spray thrower inner shell, carries out gas-liquid separation again in solution-air separate chamber 32; Carry out indirect heat exchange with the interior cooling medium of tubulation between pyrolysis liquid-vapor mixture and multiple wall, the cooling medium temperature is 60～100 ℃, can be hot water.Cooling medium in the tubulation, is discharged through tubulation cooling medium outlet 33 through the series connection tubulation by 34 inputs of tubulation cooling medium inlet again; Cooling medium in the multiple wall is entered by multiple wall cooling medium inlet 36, through multiple parietal layer, discharges through multiple wall cooling medium outlet 35 again.Liquid-vapor mixture after the heat exchange enters into the solution-air separate chamber 32 of spray thrower bottom by solution-air spacer plate 31, the pyrolysis steam of separating is sent to the bottom of deep freezer 11 by pyrolysis vapour outlet 39, and the pyrolysis liquid of separating is drained into pyrolysis liquid basin 16 by spray thrower bottom pyrolysis liquid outlet 40.Supernatant liquid in the pyrolysis liquid basin 16 is transported to the top of spray thrower again by oil pump 17, entered by circulation pyrolysis liquid inlet 38.When condensing temperature was controlled at 60～100 ℃, the pyrolysis liquid fluidity in the shell was better, was difficult for assembling and the formation obstruction in shell; The heat of process exchange is then by removing with the cooling medium indirect heat exchange of answering in the wall in the tubulation.
5. the uncooled pyrolysis steam that tubulation-come out in multiple wall spray thrower 10 bottoms is entered by deep freezer 11 bottoms, and carries out the adverse current indirect heat exchange with cooling medium in the deep freezer 11, and temperature is 0～10 ℃, and heat-eliminating medium is cooling agent or cold water.Cooling medium is added by deep freezer 11 tops, and flow out the bottom.Gas is discharged by deep freezer 11 tops like the uncooled formation aerosol.Gas carries out static by static trap 12 tops inputs and captures uncooled gas like this uncooled aerosol.The pyrolysis liquid of collecting is flow in the pyrolysis liquid basin 16 by the bottom of static trap 12, does not coagulate pyrolysis gas and is then delivered to by the side lower part pneumatic outlet of static trap and carry out drying in the moisture eliminator 13.The pyrolysis liquid of collecting in the pyrolysis liquid basin 16 is the liquid fuel of gained.
6. the non-condensable gas of being sent into by moisture eliminator 13 bottoms is dry in kiln, be transported to compressor 14 compressions, dehumidifying by the top again after, store in the gas holder 15.The dry gas of gas holder 15 through gas meter 18 quantitatively after stably to riser tube burner 1 delivery of fuel gas or outer confession.
The present invention not only provides a kind of method of utilizing steam explosion stalk fermented residuum to produce high-quality liquid fuel, and the equipment that obtains high liquid yield bio oil is provided.The liquid fuel productive rate height that this pyrolytic process method is obtained, oxygen level is low, calorific value is high, good stability.The raw material of the inventive method not only can be steam explosion stalk fermented residuum, also can be stalk fermentation residuum and other biological fermentation residuum (as the poor slag etc. of making wine).The pyrolysis feed of pyrolytic reaction device of the present invention also can adopt agricultural wastes and forestry processing wastes such as straw, wheat straw, maize straw, corn cob, beanstalk, jowar stalk, bagasse, cotton stalk, as yule logs, wood chip, sawdust, leaf etc.
Stalk vapour is quick-fried, the residuum after the fermentative processing, and the pyrolysis liquid casting yield that obtains by rotation sieve plate pyrolyzer of the present invention can reach 55～70%, and the pyrolysis oil calorific value is 22～27MJ/Kg, and the pyrolysis oil acid content also reduces greatly.
Description of drawings
Fig. 1 rotation sieve plate of the present invention fast pyrolysis process synoptic diagram.
Fig. 2 rotation sieve plate of the present invention pyrolyzer synoptic diagram.
Fig. 3 rotation sieve plate of the present invention and static agitation slurry structural representation.
The two-stage screw feeding device synoptic diagram of Fig. 4 apparatus of the present invention.
The tubulation of Fig. 5 apparatus of the present invention-multiple wall spray thrower structural representation.
Reference numeral
1. riser tube burner 2. fume dust removers 3. two-stage screw feeding devices
4. hot sand storehouse 5. rotation sieve plate pyrolyzer, 6. gas-solid quick disconnectors
7. sand coke bin 8. spirals send coke installation 9. cyclone filters
10. tubulation-multiple wall spray thrower 11. deep freezers 12. static traps
13. moisture eliminator 14. compressors 15. gas holders
16. pyrolysis liquid basin 17. oil pumps 18. gas meters
19. motor 20. rotating shafts 21. static agitation slurry
22. rotation sieve plate 23. sieve apertures 24. stalk feed bins
25. first step self-conveyor feed 26. air sealing valves 27. second stage self-conveyor feeds
28. multiple parietal layer 29. gas-liquid grid distributors 30. condensation tubulations
31. solution-air spacer plate 32. solution-air separate chambers 33. tubulation cooling mediums outlet
34. tubulation cooling medium outlet 35. multiple wall cooling medium outlet 36. multiple wall cooling medium inlets
The 39. pyrolysis vapour outlets 37. pyrolysis steam-in 38. circulation pyrolysis liquid enter the mouth
40. pyrolysis liquid outlet
Embodiment
Embodiment 1: wheat straw
Wheat straw is quick-fried through vapour, remainder contained C after fermentative processing removed hemicellulose and part Mierocrystalline cellulose respectively, the residuum that the H value is higher, through after the drying and crushing, be added in the stalk feed bin, send into rotation sieve plate pyrolyzer by the two-stage screw feeding device, and with the hot sand that comes self-heating sand storehouse at rotation sieve plate contact heat transfer, pyrolysis, not pyrolytic wheat straw and semicoke, hot sand transmits to subordinate's rotating screen plate step by step, conduct heat, pyrolysis, formed semicoke enters in the gas one solid quick disconnector with hot sand with pyrolysis steam and separates, the pyrolysis steam of separating enters into cyclone filter and further removes charred ashes, clean pyrolysis steam enters rapid condensation in tubulation-multiple wall spray thrower again, the pyrolysis steam that does not coagulate passes through deep freezer again, pyrolysis liquid is collected in the further condensation of static trap, the pyrolysis liquid of pyrolysis liquid basin, the i.e. liquid fuel of gained are stored in collection.Gu semicoke, sand by gas-quick disconnector and cyclone filter are collected send coke installation to be sent in the riser tube by spiral and burn.The pyrolysis gas that does not coagulate after capture of process static and the drying is stored in the gas holder through overdraft, dehumidification.Dry gas in the gas holder burns through sending in the riser tube after quantitative, comes heat hot sand, and is stored in the hot sand storehouse by the collected hot sand of the cyclonic separator at riser tube top.
Rotation sieve plate pyrolyzer internal diameter is 30cm, high 1m, and the sieve plate number of plies is 5 layers, spacing is 10cm.The wheat straw particle diameter is less than 0.5mm, send in the rotation sieve plate pyrolysis reactor, pyrolysis temperature is 480 ℃, reaction pressure is 0～0.002MPa (gauge pressure), rotation sieve plate pyrolyzer to the gas residence time of cyclone filter section less than 2 seconds, solid retention time in the rotation sieve plate pyrolyzer is 5～20 seconds, the ratio of mixture of hot sand and wheat straw residuum is 8: 1 (weight ratio), the riser tube temperature of combustion is 750～800 ℃, spray thrower and deep freezer temperature are respectively 60～65 ℃ and 5～10 ℃, and liquid yield is 56.2wt%, and the bio oil calorific value is 23.1MJ/kg, acidity is lower, and the pH value is 3.8.
Embodiment 2: maize straw
Maize straw is quick-fried through vapour, remainder contained C after fermentative processing removed hemicellulose and part Mierocrystalline cellulose respectively, the residuum that the H value is higher, through after the drying and crushing, be added in the stalk feed bin, send into rotation sieve plate pyrolyzer by the two-stage screw feeding device, and with the hot sand that comes self-heating sand storehouse at rotation sieve plate contact heat transfer, pyrolysis, not pyrolytic maize straw and semicoke, hot sand transmits to subordinate's rotating screen plate step by step, conduct heat, pyrolysis, Gu entering in gas-quick disconnector with hot sand with pyrolysis steam, separates formed semicoke, the pyrolysis steam of separating enters into cyclone filter and further removes charred ashes, clean pyrolysis steam enters rapid condensation in tubulation-multiple wall spray thrower again, the pyrolysis steam that does not coagulate passes through deep freezer again, pyrolysis liquid is collected in the further condensation of static trap, the pyrolysis liquid in the pyrolysis liquid basin, the i.e. liquid fuel of gained are stored in collection.Gu semicoke, sand by gas-quick disconnector and cyclone filter are collected send coke installation to be sent in the riser tube by spiral and burn.The pyrolysis gas that does not coagulate after capture of process static and the drying is stored in the gas holder through overdraft, dehumidification.Dry gas in the gas holder burns through sending in the riser tube after quantitative, comes heat hot sand, and is stored in the hot sand storehouse by the collected hot sand of the cyclonic separator at riser tube top.
Rotation sieve plate pyrolyzer internal diameter is 30cm, high 1m, and the sieve plate number of plies is 5 layers, spacing is 10cm.The wheat straw particle diameter is less than 0.5mm, send in the rotation sieve plate pyrolysis reactor, pyrolysis temperature is 500 ℃, reaction pressure is 0～0.002MPa (gauge pressure), rotation sieve plate pyrolyzer to the gas residence time of cyclone filter section less than 2 seconds, solid retention time in the rotation sieve plate pyrolyzer is 5～20 seconds, the ratio of mixture of hot sand and wheat straw residuum is 8.5: 1 (weight ratio), the riser tube temperature of combustion is 750～800 ℃, spray thrower and deep freezer temperature are respectively 60～65 ℃ and 5～10 ℃, and liquid yield is 60.3wt%, and the bio oil calorific value is 23.8MJ/kg, acidity is lower, and the pH value is 3.7.
Claims (10)
1. the device of a thermolysis preparing liquid fuel from steam explosion stalk fermented residue, the parts composition that is connected by pipeline comprises: riser tube burner (1), fume dust remover (2), two-stage screw feeding device (3), hot sand storehouse (4), rotation sieve plate pyrolyzer (5), gas-solid quick disconnector (6), sand coke bin (7), spiral send coke installation (8), cyclone filter (9), tubulation-multiple wall spray thrower (10), deep freezer (11), static trap (12), moisture eliminator (13), compressor (14), gas holder (15), pyrolysis liquid basin (16), oil pump (17), gas meter (18); It is characterized in that:
The bottom of one riser tube burner (1) has the wind inlet one time, the inside at the riser tube burner (1) on wind inlet top is provided with grid distributor, be positioned on the wall of riser tube burner (1) of grid distributor top and have the burnt import of a sand, and send the outlet of coke installation (8) to be connected by pipeline and spiral; Have the import of pyrolysis dry gas in the burnt import of the sand of riser tube burner (1) top, the middle part of riser tube burner (1) is provided with the secondary air inlet; Riser tube burner (1) top exit is connected with the first step cyclonic separator top inlet mouth of fume dust remover (2);
The first step cyclonic separator outlet at bottom of one fume dust remover (2) is connected with the top inlet in hot sand storehouse (4), first step cyclonic separator top exit is connected with cyclonic separator top, the second stage inlet mouth of fume dust remover (2), cyclonic separator bottom, the second stage is provided with ash discharging hole, and the top is hot flue gas discharge opening;
One hot sand storehouse (4) outlet at bottom adds the sand mouth with the top of rotation sieve plate pyrolyzer (5) and is connected, rotation sieve plate pyrolyzer (5) crown center is equipped with motor (19), and its top is provided with the stalk charging opening and is connected with second stage self-conveyor feed (27) outlet of two-stage screw feeding device (3); Rotation sieve plate pyrolyzer (5) outlet at bottom is connected with gas-solid quick disconnector (6) top inlet;
The top of one gas-solid quick disconnector (6) is provided with two pneumatic outlets, and is connected with the middle and upper part inlet mouth of cyclone filter (9), and gas-solid quick disconnector (6) outlet at bottom is connected with the top inlet of sand coke bin (7); Another import that is positioned at sand coke bin (7) upper lateral part is connected with the outlet at bottom of cyclone filter (9), and sand coke bin (7) outlet at bottom directly is connected in spiral and send in coke installation (8) import;
The air outlet, top of one cyclone filter (9) is connected with the pyrolysis steam-in (37) at tubulation-multiple wall spray thrower (10) top, tubulation-multiple wall spray thrower (10) bottom pyrolysis liquid outlet (40) is connected with pyrolysis liquid basin (16) liquid inlet, top, and the pyrolysis vapour outlet (39) of tubulation-multiple wall spray thrower (10) side lower part is connected with the pyrolysis steam inlet of deep freezer (11) side lower part; Tubulation-multiple wall spray thrower (10) both sides are distributed with the import and export of cooling medium in tubulation, the multiple wall respectively;
The top of one deep freezer (11) is provided with pneumatic outlet, and be connected with the top inlet mouth of static trap (12), the outlet of pyrolysis liquid is all established in the bottom of deep freezer (11) and static trap (12), and all the liquid inlet with pyrolysis liquid basin (16) top is connected; Deep freezer (11) sidepiece is provided with the import and export of cooling medium;
One static trap (12) side lower part air outlet is connected with moisture eliminator (13) bottom air inlet, and moisture eliminator (13) air outlet, top links to each other with compressor (14) inlet mouth, and compressor (14) air outlet is connected with gas holder (15) bottom air inlet; Gas holder (15) top is provided with drain and outer air feed port, and the air outlet of gas holder (15) middle and lower part links to each other with gas meter (18) inlet mouth, and the air outlet of under meter (18) links to each other with the pyrolysis dry gas import of riser tube burner (1) middle and lower part;
One pyrolysis liquid basin (16) middle and lower part is provided with the outlet of pyrolysis liquid and is connected with oil pump (17) import, and oil pump (17) outlet is connected with the circulation pyrolysis liquid inlet at tubulation-multiple wall spray thrower (10) top; Pyrolysis liquid basin (16) bottom is provided with the relief outlet of pyrolysis liquid.
2. device according to claim 1, it is characterized in that: described two-stage screw feeding device (3) is made up of its top stalk feed bin (24) and stalk feed bin bottom first step self-conveyor feed (25), air sealing valve (26) and second stage self-conveyor feed (27), and air sealing valve (26) is positioned between the two-stage screw parts (25,27).
3. device according to claim 1 is characterized in that: the cylindrical shell of described rotation sieve plate pyrolyzer (5) is cylindricality, and its bottom is taper; The sand of adding mouth is arranged at cylindricality wall top, the pyrolyzer top has the stalk charging opening, the pyrolyzer center of top is equipped with motor (19), motor (19) links to each other with rotating shaft (20) by the sealed attachment part, be fixed with multiple rotary screen plate (22) in the rotating shaft (20), every layer of rotation sieve plate (22) gone up with a static agitation slurry (21).
4. device according to claim 3 is characterized in that: described rotation sieve plate (22) is the garden dish type, is distributed with the sieve aperture (23) that is increased gradually by center diameter to the outer rim direction on the dish; Described static agitation slurry (21) is colter shape, and itself and rotating shaft (20) loop type connect.
5. device according to claim 3 is characterized in that: the interlamellar spacing of the rotation sieve plate (22) in the described rotating shaft (20) is 10～30cm.
6. device according to claim 1 is characterized in that: the lower end, air outlet, top of described cyclone filter (9) links the barrel-shaped metal filter screen in 50～300 purpose gardens.
7. device according to claim 1, it is characterized in that: the chuck that the multiple wall of described tubulation-multiple wall spray thrower (10) is made up of two-layer cylindrical vessel, multiple wall cooling medium inlet (36) is positioned at the bottom of spray thrower, and multiple wall cooling medium outlet (35) is positioned at the top of spray thrower; The top of spray thrower is provided with the side entrance (38) of pyrolysis steam-in (37) and circulation pyrolysis liquid; The spray thrower inner shell is equipped with condensation tubulation (30), forms single passage, and its cooling medium inlet (34) is positioned at the bottom of spray thrower, and its cooling medium outlet (33) is positioned at the top of spray thrower; The top of tubulation is provided with gas-liquid grid distributor (29); The inner shell of spray thrower and the below that is positioned at condensation tubulation (30) are provided with downward-sloping solution-air spacer plate (31), the below of solution-air spacer plate is solution-air separate chamber (32), be made as two pyrolysis vapour outlets (39) in the top of solution-air separate chamber, the bottom of spray thrower, the bottom of spray thrower or solution-air separate chamber (32) is pyrolysis liquid outlet (40).
8. device according to claim 7 is characterized in that: the downward-sloping pitch angle of described solution-air spacer plate (31) is 30 °.
9. using method according to each thermolysis preparing liquid fuel from steam explosion stalk fermented residue device of claim 1～8:
Stalk fermentation residuum in the stalk feed bin (24) is quantitatively joined on the rotation sieve plate (22) by rotation sieve plate pyrolyzer (5) top by two-stage screw feeding device (3), and mix with the hot sand that comes self-heating sand storehouse (4), the weight ratio of hot sand and stalk material is 8～10: 1, pyrolysis temperature is 400～700 ℃, and pressure is 0～0.002Mpa; Mixture drops into the enterprising step heat transfer of subordinate's rotation sieve plate, pyrolysis step by step by the sieve aperture (23) on the rotation sieve plate (22); Steam, semicoke and the hot sand that pyrolysis produces is dropped in the gas-solid quick disconnector (6) by the outlet at bottom of rotation sieve plate pyrolyzer (5) together;
By the gas-solid mixture that gas-solid quick disconnector (6) top enters, sharp separation goes out pyrolysis steam, semicoke and hot sand in separator; The pyrolysis steam that carries a small amount of thin ash enters further cyclonic filter ash disposal in the cyclone filter (9) by the pneumatic outlet on separator top; Isolated Jiao of separator, ash and sand are discharged by the bottom and are entered into sand coke bin (7) together;
Hot sand, the semicoke mixture of storage in sand coke bin (7) enters spiral by its outlet at bottom and send in the coke installation (8), spiral send coke installation (8) that hot sand, semicoke mixture are transported in the riser tube burner (1) by the bottom of riser tube burner (1) to burn, the temperature of combustion of riser tube is 750～850 ℃, and pressure is 0～0.002Mpa; The hot sand of heating and hot flue gas are through first step cyclonic separator in the fume dust remover (2) at riser tube top, the hot sand that cyclonic separation is come out is stored in the hot sand storehouse (4), and the hot flue gas that carries a small amount of thin ash passes through second stage cyclonic separator dedusting in the fume dust remover (2) again, discharged by this cyclonic separator top, the collected thin ash of cyclonic separation is discharged by ash discharging hole;
The pyrolysis steam that comes out in cyclone filter (9) top enters spray thrower by tubulation-multiple wall spray thrower (10) top gas inlet (37), carries the circulation pyrolysis liquid of coming also to enter spray thrower by top circulation pyrolysis liquid inlet (38) by oil pump (17) simultaneously; Pyrolysis steam of being come in by the spray thrower top and circulation pyrolysis liquid direct contact heat-exchanging in gas-liquid grid distributor (29) makes pyrolysis steam rapid condensation, and with pyrolysis steam and be advanced into the spray thrower inner shell, carries out gas-liquid separation again in solution-air separate chamber (32); Carry out indirect heat exchange with the interior cooling medium of tubulation between pyrolysis liquid-vapor mixture and multiple wall, the cooling medium temperature is 60～100 ℃, liquid-vapor mixture after the heat exchange enters into the solution-air separate chamber (32) of spray thrower bottom by solution-air spacer plate (31), the pyrolysis steam of separating is sent to the bottom of deep freezer (11) by pyrolysis vapour outlet (39), and the pyrolysis liquid of separating is drained into pyrolysis liquid basin (16) by spray thrower bottom pyrolysis liquid outlet (40); Supernatant liquid in the pyrolysis liquid basin (16) is transported to the top of spray thrower again by oil pump (17), entered by circulation pyrolysis liquid inlet (38); When condensing temperature was controlled at 60～100 ℃, the heat of process exchange was then by removing with the cooling medium indirect heat exchange of answering in the wall in the tubulation;
The uncooled pyrolysis steam that tubulation-come out in multiple wall spray thrower (10) bottom is entered by deep freezer (11) bottom, and carry out the adverse current indirect heat exchange with cooling medium in the deep freezer (11), temperature is 0～10 ℃, gas is discharged by deep freezer (11) top like the uncooled formation aerosol, and gas carries out static by the input of static trap (12) top and captures uncooled gas like this uncooled aerosol; The pyrolysis liquid of collecting is flow in the pyrolysis liquid basin (16) by the bottom of static trap (12), does not coagulate pyrolysis gas and is then delivered in the moisture eliminator (13) by the side lower part pneumatic outlet of static trap and carry out drying; The pyrolysis liquid of collecting in the pyrolysis liquid basin (16) is the liquid fuel of gained.
10. method according to claim 9 is characterized in that: the described non-condensable gas of being sent into by moisture eliminator (13) bottom is dry in kiln, be transported to compressor (14) compression, dehumidifying by the top again after, store in the gas holder (15); The dry gas of gas holder (15) through gas meter (18) quantitatively after stably to riser tube burner (1) delivery of fuel gas or outer confession.
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| CNB2005100111043A CN100357396C (en) | 2005-01-05 | 2005-01-05 | Method and device for thermolysis preparing liquid fuel from steam explosion stalk fermented residue |
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| CNB2005100111043A CN100357396C (en) | 2005-01-05 | 2005-01-05 | Method and device for thermolysis preparing liquid fuel from steam explosion stalk fermented residue |
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