CN1928013A - Biomass deep dehydration carbonization continuous processing technology and device thereof - Google Patents
Biomass deep dehydration carbonization continuous processing technology and device thereof Download PDFInfo
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Abstract
Continuous biomass deeply dewatering and carbonizing process and apparatus are disclosed. The technological process includes the steps of deeply dewatering biomass to separate out water at 120-160 deg.c with external heat source, and carbonizing biomass at 300-500 deg.c to obtain biomass charcoal and pyrolytic fuel gas. The apparatus includes one drier and one carbonizing unit with material inlet connected to the outlet of the drier and sandwiched heat exchange cavity connected to that of the drier. Inside the carbonizing unit, there is also one gas assistant jetting device for controlling the reaction temperature in the carbonizing process. The present invention has high heat efficiency, high heat value of the pyrolytic gas and high biomass charcoal yield.
Description
Technical field
The invention belongs to the biomass energy technology field, relate to and utilize the carbon containing biomass material to prepare high-temperature gasification with the biomass charcoal of high-energy-density with burn the method and the equipment of pyrolysis gas with the high heating value volatile combustible that gaseous form exists, refer to a kind of biomass deep dehydration carbonization continuous processing technology and equipment thereof particularly, this equipment is the treatment facility in early stage that synthetic gas is made in the biomass high-temperature gasification.
Background technology
Biomass are carbonaceous materials that plant generates by photosynthesis, and reserves are abundant, are a kind of reproducible energy.Under the situation that petroleum resources reduce day by day, efficiently utilizing reproducible biomass energy is extremely urgent problem.Gasifying biomass is produced the problem that various synthetic gas are engineering technical personnel's primary studies always.
Often carbonaceous material is broken into smaller particles on the engineering, at high temperature carries out gasification reaction production of synthetic gas in next life.The gasification process of the carbonaceous material that exists can be divided into fixed bed gasification method, fluidized-bed gasification method and entrained flow gasification method three major types substantially at present.But Mierocrystalline cellulose and xylogen are more in the biomass material, and toughness is stronger, on the one hand its be not easy by physical method pulverize for be suitable for above-mentioned gasification process than small-particle, its water content is bigger on the other hand, generates the H of no calorific value in the gasification easily
2O has diluted gasification product, has reduced the quality of synthetic gas.Therefore, on the engineering generally be not simply with aforesaid method with the biomass direct gasification, but destroy the method for the structure of Mierocrystalline cellulose and xylogen in the biomass by pyrolysis, make biomass material change into biomass charcoal and incendivity pyrolysis gas, again biomass charcoal is ground to smaller particles and carry out high-temperature gasification, produce the higher synthetic gas of calorific value.
Yet the initial water content of biomass material is about about 30%, through conventional drying or air-dry after the water content of biomass material generally also have 15～20%.Prior biological matter charcoal metallization processes is general only carries out conventional air-dry or drying treatment to biomass material, the water ratio of biomass material is still higher, the moisture content that such wet stock is evaporated in carbonization process remains in the incendivity pyrolysis gas that produces after the charing, both reduce the calorific value of pyrolysis gas, reduced the thermo-efficiency of system again because of its heat that absorbs the charing system.
Publication number is that the Chinese invention patent ublic specification of application of CN1710023A has proposed a kind of low-tar biomass gasifying method and device.This method at first makes biomass generation carbonization reaction generate pyrolysis gas and biomass charcoal, makes biomass charcoal generation reduction reaction make synthetic gas again.The non-oxidation agent in the carbonization process of biomass of this method feeds, adopt outer thermal source to give the heat supply of carbonization reaction device, though reduced the self-heating quantity combusted of biomass material, but the biomass material that carries out the charing processing does not have the deep dehydration process, the moisture content that moisture content that this humidogene raw material of substance is contained and carbonization reaction are produced all retains in the pyrolysis gas of carbonization process generation, cause that the useless one-tenth portioning of pyrolysis gas increases, calorific value reduces, and is unfavorable for the further utilization of pyrolysis gas.This device adopts outer thermal source to regulate the temperature of control carbonization reaction device singlely, and the temperature regulation effect is relatively poor, hysteresis quality is obvious, and particularly the carbonization reaction device needs preheating for a long time under the driving operating mode, exists to start difficulty, the low defective of thermo-efficiency.
Publication number is to have proposed a kind of method and back fire-biomass carbonated gas generating stove of producing biomass carbonated gas in the Chinese invention patent ublic specification of application of CN1710022A.This producer divides two-layer layout up and down with the carbonization reaction device of biomass, and the oxidising process of biomass material, reduction process and carbonization process concentrate in the burner hearth and carry out.Carbonization reaction device upper strata combustion parts biomass, the high-temperature tail gas that burning produces feeds carbonization reaction device lower floor, biomass charcoalization with carbonization reaction device lower floor, the gas of calorific value during pyrolysis gas that is produced and upper strata combustion tail gas are mixed into, be sucked out outside the carbonization reaction device, the biomass charcoal that is produced is discharged from lower floor.This producer only utilizes a part of biomass material of burning to provide heat for charing other biological raw material, in retort process, there is not material to stir measure yet, carbonization reaction device lower floor produces bonding because of local superheating easily, and carbonization process generates in the inflammable gas and mixes the H that produces because of combustion tail gas
2O, CO
2Measure morely, less because of the output of natural biology matter charcoal, the product calorific value of the inflammable gas of carbonization process is not high, and charing system production efficiency is on the low side.
Summary of the invention
Purpose of the present invention be exactly to provide a kind of in carbonization process biomass material adapt to that wide, temperature of reaction is convenient to regulate and control, charing equipment thermal efficiency height, final carbonizing production in pyrolysis gas calorific value height, biomass deep dehydration carbonization continuous processing technology and equipment thereof that biomass charcoal output is high.
For achieving the above object, the biomass deep dehydration carbonization continuous processing technology that the present invention is designed, the outer thermal source of main employing provides heat for the biomass material in asher and the moisture eliminator successively continuously.The drying process controlled temperature makes the biomass material deep dehydration in 120～160 ℃ scope, the moisture content of being separated out is excluded, and can not enter the carbonization reaction system.The carbonization process controlled temperature makes the biomass generation carbonization reaction of deep dehydration in 300～500 ℃ scope, be transformed into biomass charcoal and incendivity pyrolysis gas, and guarantees the calorific value height of pyrolysis gas, the output height of charcoal.Its technological process comprises the steps:
1) at first the biomass under the state of nature are chosen and cleared up, remove the waste material that wherein dirt, hard thing, impurity etc. do not meet production requirement, it is air-dry that the material of the selected suitable charing that goes out carries out routine.The original water ratio of biomass material by the air-dry external moisture content that can tentatively remove in the material of routine, is controlled in 15～20% the scope water ratio of material generally about 30%.
2) then the air-dry material of routine being carried out the machinery chopping handles, the particle diameter of material particles is controlled in the scope of 5～80mm, for example cutting into length is that 5～80mm, width or diameter are the strip particle of 5～10mm, both be convenient to the conveying of material, also help material and be heated evenly in dehydration, moisture content is more easily separated out.
3) again the material particles of chopping is directly sent into and carried out deep dehydration in the moisture eliminator and handle, control the temperature of moisture eliminator in 120～160 ℃ scope by regulating outer thermal source, under the propulsive state of continuously stirring, most of moisture content in the material particles was both separated out quickly, pyrolytic reaction does not take place again, final its water ratio is reduced in 8～10% the scope, and the moisture content that volatilizes is discharged outside the moisture eliminator.
4) at last the material particles of deep dehydration is sent into and carried out charing in the asher and handle, control the temperature of asher in 300～500 ℃ scope by regulating outer thermal source, under the propulsive state of continuously stirring, make material particles that carbonization reaction fully take place, generating solid-state biomass charcoal and major ingredient is CO, H
2Incendivity pyrolysis gas, and the tar of minute quantity.Final biomass charcoal is discharged from the biomass charcoal outlet of asher bottom, and incendivity pyrolysis gas is discharged from asher top pyrolysis gas outlet.
In the above-mentioned biomass deep dehydration carbonization continuous processing technology, preferably make the spontaneous combustion of partial material particle or make the material particles temperature reduction way, cooperate outer thermal source to come the temperature of Collaborative Control asher to remain in 300～500 ℃ the scope by adding the gaseous state auxiliary agent.Like this can be at any time according to the temperature regime of asher, feed different gaseous state auxiliary agents such as oxygen, air makes the spontaneous combustion of partial material particle, or Low Temperature Steam, freezing air etc. make material particles cooling, thereby regulate and control the temperature of reaction of asher in time, easily and flexibly.
In the above-mentioned biomass deep dehydration carbonization continuous processing technology, the stirring of material particles in moisture eliminator advances the residence time preferably to be controlled in the scope of 600～1200s, can separate out fast to guarantee the most of moisture content in the wet stock.The stirring of material particles in asher advances the reaction times preferably to be controlled in 200～1000s scope, to guarantee fully charing of material particles.
In the above-mentioned biomass deep dehydration carbonization continuous processing technology, the air pressure in moisture eliminator and the asher preferably all is controlled in the scope of 3.0～4.0MPa, can effectively suppress CO in the biomass charcoal process like this
2With the growing amount of bio-crude oil, impel CO and H in the incendivity pyrolysis gas that biomass carbonated process produces
2More.
For realizing the custom-designed biomass deep dehydration carbonization continuous processing apparatus of above-mentioned technology, comprise moisture eliminator and asher.Moisture eliminator has moisture eliminator material inlet, moisture eliminator screw feeder, moisture eliminator material outlet and moisture eliminator steam outlet, the housing of moisture eliminator is provided with the moisture eliminator interlayer heat exchange cavity that passes through for outer thermal source medium, and the two ends of moisture eliminator interlayer heat exchange cavity are respectively arranged with outer thermal source medium import of moisture eliminator and the outer thermal source media outlet of moisture eliminator.Asher has asher material inlet, asher stirring rake, asher coke export and asher pyrolysis gas outlet, the housing of asher is provided with the asher interlayer heat exchange cavity that passes through for outer thermal source medium, and the two ends of asher interlayer heat exchange cavity are respectively arranged with outer thermal source medium import of asher and the outer thermal source media outlet of asher.For sealing is connected, be to seal to be connected between the outer thermal source medium import of moisture eliminator and the outer thermal source media outlet of asher between moisture eliminator material outlet and the asher material inlet.
Further, outer thermal source medium import of above-mentioned moisture eliminator and the outer thermal source media outlet of moisture eliminator are separately positioned on the side near moisture eliminator material outlet and moisture eliminator material inlet.Outer thermal source medium import of above-mentioned asher and the outer thermal source media outlet of asher are separately positioned on the side near asher coke export and asher material inlet.Like this, the flow direction of outer thermal source is opposite with the direction of motion of material particles in moisture eliminator and the asher, material particles increases gradually along the heat that its direction of motion obtained, outer thermal source is just in time corresponding with drying treatment and the needed heat of carbonization reaction with this countercurrent heat exchange method of material particles, thereby can make good use of outer thermal source most economically.
Further, the intracavity bottom of above-mentioned asher is provided with the arc surfaced burner plate, the arc angle of arc surfaced burner plate is generally 70～110 °, is evenly equipped with gaseous state auxiliary agent nozzle on the arc surfaced burner plate, and gaseous state auxiliary agent nozzle is connected with the gaseous state auxiliary agent inlet pipe of introducing from outside, asher bottom.Like this, can feed the temperature that different gaseous state auxiliary agents is in time controlled asher according to temperature regimes different in the asher working process.When outer thermal source heat is not enough to provide the heat that the biomass raw material particle charing needs in the asher, can bubbling air, auxiliary agent such as oxygen, high-temperature water vapor, combustion parts feed particles on the arc surfaced burner plate, heat other feed particles in the asher, the part heat that provides biomass charcoalization to need.Particularly under asher driving operating mode, at arc surfaced burner plate up-igniting part material particle, can the rapid heating asher to the temperature of design, impel the operation of asher to reach stable state rapidly, thereby effectively solve the asher driving and enter the slow difficult problem of normal operating conditions, simplify the startup procedure of asher.When outer thermal source heat greater than asher in the biomass raw material particle charing need heat the time, can feed auxiliary agents such as water at low temperature steam, reduce the local temperature on the arc surfaced burner plate, can prevent that the arc surfaced burner plate from burning, can effectively regulate the temperature of carbonization reaction again.When having tar to produce on the arc surfaced burner plate and during deposition, can feed high-temperature water vapor and impel on the arc surfaced burner plate agglutinating tar to carry out secondary to decompose, generate micromolecular hydrocarbon polymer.
Further, be formed with the arc surfaced enclosed cavity between above-mentioned arc surfaced burner plate and the asher bottom, above-mentioned gaseous state auxiliary agent inlet pipe is connected with gaseous state auxiliary agent nozzle by the arc surfaced enclosed cavity.Like this, the gaseous state auxiliary agent is assembled below the arc surfaced burner plate after again from gaseous state auxiliary agent nozzle evenly the ejection, the gaseous state auxiliary agent is played a role better.Above-mentioned gaseous state auxiliary agent nozzle preferably adopts calotte formula structure, is made of nozzle pipe and the nozzle bubble-cap that is installed in the nozzle pipe head.Like this, can prevent effectively that material particles and tar from spray nozzle clogging, helping regulating the carbonization reaction temperature more neatly, guarantee the asher works better.
Compared with prior art, the present invention has the advantage of following several respects:
1. technology of the present invention is at first carried out the forced drying deep dehydration to biomass raw material particle and is handled under 120～160 ℃ temperature condition, the moisture content that contains in the feed particles is separated out as much as possible, and keep feed particles that pyrolytic reaction does not take place under this temperature condition or takes place less, the moisture content of being separated out is directly discharged outside the moisture eliminator, again feed particles is sent into asher and reacts.Like this, the temperature of feed particles is in different stage stepped control, and it is stable not only to regulate maintenance easily, and can effectively avoid the influence of moisture content to the feed particles carbonization reaction, the calorific value of the pyrolysis gas that significantly improves carbonization reaction and produced has also improved the charing device heat efficiency simultaneously.
2. it is asher and moisture eliminator heat supply that technology of the present invention mainly adopts outer thermal source, the heat combustion material particle for providing carbonization reaction to need is provided as far as possible, thereby is effectively reduced combustion material H that particle is produced
2O and CO
2Content, improved CO and H in the pyrolysis gas that carbonization reaction generated
2Concentration, and then improved the calorific value of the pyrolysis gas that is produced, also improved the output of the biomass charcoal that is produced.
3. equipment of the present invention is provided with the arc surfaced burner plate in asher, the arc surfaced burner plate is provided with gaseous state auxiliary agent nozzle, can import different gaseous state auxiliary agents according to the temperature regime of asher, thereby can regulate and control the temperature of asher easily.Impel its spontaneous combustion as input air, oxygen, high-temperature water vapor, or input freezing air, water at low temperature steam reduces its temperature of reaction, or spray into high-temperature steam and impel tar to decompose, reduce the bonding of tar on asher, guarantee normal, the efficient operation of equipment.
This shows, charing equipment thermal efficiency height of the present invention, the carbonization reaction temperature is convenient to regulate and control, and water vapor and tar content are less, and the pyrolysis gas calorific value that carbonization reaction generates is higher.The present invention is not only applicable to the charing of general timber, cotton stalk, straw biolobic material raw material and handles, and is suitable for solid-state organic gasified raw materials such as domestic refuse, industrial refuse.
Description of drawings
Fig. 1 is a kind of structural representation of biomass deep dehydration carbonization continuous processing apparatus;
Fig. 2 is the sectional structure synoptic diagram of moisture eliminator among Fig. 1;
Fig. 3 is the sectional structure synoptic diagram of asher among Fig. 1;
Fig. 4 is the structure for amplifying synoptic diagram of arc surfaced burner plate among Fig. 3;
Fig. 5 is the structure for amplifying synoptic diagram of gaseous state auxiliary agent nozzle among Fig. 3.
Embodiment
Below in conjunction with the drawings and specific embodiments biomass deep dehydration carbonization continuous processing technology of the present invention and equipment thereof are described in further detail:
Biomass deep dehydration carbonization continuous processing apparatus shown in the figure is mainly connected to form successively by cutting unit 2, moisture eliminator 6, asher 12.Cutting unit 2 is provided with cutting unit material inlet 1 and cutting unit material outlet 3.
Moisture eliminator 6 is provided with moisture eliminator screw feeder 17, moisture eliminator material outlet 7 and the moisture eliminator steam outlet 9 of moisture eliminator material inlet 4, motor 16 drivings.The housing of moisture eliminator 6 is made of shell 18 and inner bag 20, forms the moisture eliminator interlayer heat exchange cavity 19 that passes through for outer thermal source medium between shell 18 and the inner bag 20.The two ends of moisture eliminator interlayer heat exchange cavity 19 are respectively arranged with outer thermal source medium import 8 of moisture eliminator and the outer thermal source media outlet 5 of moisture eliminator, the outer thermal source medium import 8 of moisture eliminator is arranged on the side near moisture eliminator material outlet 7, and the outer thermal source media outlet 5 of moisture eliminator is arranged on a side of moisture eliminator material inlet 4.
Asher 12 is provided with asher stirring rake 25, asher coke export 13 and the asher pyrolysis gas outlet 15 of asher material inlet 10, motor 21 drivings, be provided with material baffle 26 near the asher coke export 13, to guarantee that material particles is through discharging from asher coke export 13 after the abundant charing again.The housing of asher 12 also is a sandwich structure, is made of outer shell 29 and bladder layer 27, forms the asher interlayer heat exchange cavity 28 that passes through for outer thermal source medium between outer shell 29 and the bladder layer 27.The two ends of asher interlayer heat exchange cavity 28 are respectively arranged with outer thermal source medium import 14 of asher and the outer thermal source media outlet 11 of asher, the outer thermal source medium import 14 of asher is arranged on the side near asher coke export 13, and the outer thermal source media outlet 11 of asher is arranged on a side of asher material inlet 10.
Above-mentioned cutting unit material outlet 3 is connected as a single entity with moisture eliminator material inlet 4, and moisture eliminator material outlet 7 is connected with 10 sealings of asher material inlet, and the outer thermal source medium import 8 of moisture eliminator is connected with outer thermal source media outlet 11 sealings of asher.
The outside of the shell 18 of above-mentioned moisture eliminator 6 and the outer shell 29 of asher 12 is coated with lagging material, to reduce outer thermal source such as the calorific loss of hot flue gas in transmission course.Lagging material is outward again with the iron sheet parcel, to guarantee its physical strength.Above-mentioned moisture eliminator interlayer heat exchange cavity 19 and asher interlayer heat exchange cavity 28 also can replace with film mode tube screen formula heat transfer tube or spiral wound form heat transfer tube, as long as its conduction of satisfying heat requires.
The intracavity bottom of above-mentioned asher 12 is equipped with arc surfaced burner plate 23, the arc angle of arc surfaced burner plate 23 generally is designed to 70～110 °, the arc angle of arc surfaced burner plate 23 is 90 ° in the present embodiment, and its area accounts for 1/4th of asher inner chamber area.Be evenly equipped with gaseous state auxiliary agent nozzle 22 on the arc surfaced burner plate 23, gaseous state auxiliary agent nozzle 22 is a calotte formula structure, and it is made of nozzle pipe 31 and the nozzle bubble-cap 32 that is installed in nozzle pipe 31 heads, can avoid material particles and tar with spray nozzle clogging.Be formed with arc surfaced enclosed cavity 30 between arc surfaced burner plate 22 and asher 12 bottoms, the gaseous state auxiliary agent inlet pipe of introducing from outside, asher 12 bottoms 24 is connected with gaseous state auxiliary agent nozzle 22 by arc surfaced enclosed cavity 30.
The principle of work of biomass deep dehydration carbonization continuous processing apparatus of the present invention is such:
Be about 15～20% biomass material through cleaning, air-dry, water ratio and enter cutting unit 2 from cutting unit material inlet 1, be cut into the particle that length 5～80mm, width or diameter are 5～10mm, discharge from cutting unit material outlet 3,, enter in the moisture eliminator 6 by moisture eliminator material inlet 4.
Start moisture eliminator motor 16, drive moisture eliminator screw feeder 17 transferring raw material particles, control enters the hot exhaust gas volumn in the moisture eliminator interlayer heat exchange cavity 19, the temperature of moisture eliminator 6 is remained in 120～160 ℃ the scope, the residence time of material particles in moisture eliminator 6 remains 600～1200s, moisture content in the feed particles volatilizees fast, water ratio is reduced to about 8～10%, water vapor is discharged from moisture eliminator steam outlet 9, the feed particles of depth drying is discharged from moisture eliminator material outlet 7, by asher material inlet 10, enter in the asher 12.
Start asher motor 21, drive asher stirring rake 25 and stir feed particles, control enters the hot exhaust gas volumn in the asher interlayer heat exchange cavity 28, the temperature of asher 12 is remained in 300～500 ℃ the scope, the residence time of material particles in asher 12 is 200～1000s, feed particles generation carbonization reaction, the biomass charcoal that is generated after the charing is crossed material baffle 26, discharge from asher coke export 13, the pyrolysis gas that is generated is then discharged by asher pyrolysis gas outlet 15.
Adopt hot flue gas to moisture eliminator 6 and asher 12 indirect heat exchanges.The thermal source medium import 14 outside asher of hot flue gas enters asher interlayer heat exchange cavity 28, thermal source media outlet 11 discharges outside asher after the heat exchange, thermal source medium import 8 enters moisture eliminator interlayer heat exchange cavity 19 outside moisture eliminator again, thermal source media outlet 5 discharges outside moisture eliminator after the heat exchange.Hot flue gas is given asher 12 and moisture eliminator 6 heating successively according to the needs of temperature height, and its flow direction is opposite with the direction of motion of feed particles, and this reverse heat-exchange mode can significantly improve the utilising efficiency of hot flue gas.
Can in asher 12, carry the gaseous state auxiliary agent at any time according to thermoregulator needs.The gaseous state auxiliary agent accumulates in the arc surfaced enclosed cavity 30 between arc surfaced burner plate 23 and asher 12 bottoms by gaseous state auxiliary agent inlet pipe 24 earlier, sprays into by gaseous state auxiliary agent nozzle 22, to adjust the interior temperature of asher 12 again.Specifically, when the temperature in the asher 12 is lower than design temperature, can bubbling air, oxygenant such as oxygen, make the part material particle burning on the arc surfaced burner plate 23, improve the temperature of asher 12, for other feed particles provide charing required energy; When the temperature in the asher 12 is higher than design temperature, can feed cold air, cold steam, reduce the local temperature of arc surfaced burner plate 23, prevent that it from burning; When on the arc surfaced burner plate 23 tar deposition being arranged, can feed elevated temperature heat steam, make agglutinating tar secondary decomposition on it, thereby guarantee the quality of final carbonizing production.Moisture eliminator 6 and asher 12 can be worked under normal pressure, also the air pressure in it can be controlled in the scope of 3.0～4.0MPa, to suppress CO in the biomass charcoal process
2With the growing amount of bio-crude oil, impel biomass pyrolytic to produce more CO and H
2, but the big more cost of pressure is high more.
Below be the several specific embodiments that utilize technology of the present invention and device processes biomass:
Embodiment one: be the charing raw material with the withy.The withy selection back of collecting is cleaned, is removed earth and other impurity in the withy raw material, with raw material air-dry to material water ratio in 15～20% scope.Material after air-dry is packed in the cutting unit, and material is cut into the particle of particle diameter 5～80mm.Material after the cutting is directly imported moisture eliminator, start the moisture eliminator motor, material advances under the effect of spiral screw feeder, feeds hot flue gas heating moisture eliminator simultaneously in moisture eliminator, the actuator temperature that keeps dry is 130～150 ℃, and material residence time in moisture eliminator is 700～1000s.Dried material is directly imported asher, start the asher motor, material moves to outlet under the effect of stirring rake, in asher, feed hot flue gas heating asher simultaneously, keeping the asher temperature is 300～500 ℃, and material residence time in asher is 600～1000s, and pyrolytic reaction takes place in asher material, the gaseous product that pyrolysis produces is discharged from pyrolysis gas outlet, and the solid product charcoal is discharged from the coke discharge outlet.Learn that after testing to the charging of every 1kg withy, the moisture content that moisture eliminator is discharged is about 0.0863kg, the charcoal of generation is about 0.13kg, and ash is about 0.0233kg, and the pyrolysis gas of generation is about 0.7590kg.Percentage calculation by volume, the each component in the pyrolysis gas is: H
2-10.86%, CO
2-9.06%, CO-30.21%, H
2O-27.69%, CH
4-10.86%, N
2-0.34%, carbon two above organic components and other inorganic components-10.98%.
Embodiment two: raw material is changed to cotton stalk.The cotton stalk selection back of collecting is cleaned, removed earth and other impurity in the cotton haulm raw material.With raw material air-dry to material water ratio in 15～20% scope.Material after air-dry is packed in the cutting unit, and material is cut into the particle that particle diameter is 5～80mm.The actuator temperature that keeps dry is 140～160 ℃, and material residence time in moisture eliminator is 900～1200s.Keeping the temperature of asher is 300～500 ℃, and the residence time of material in asher is 200～800s.Learn that after testing to the charging of every 1kg cotton stalk, the moisture content that moisture eliminator is discharged is about 0.1553kg, the charcoal of generation is about 0.17kg, and ash is about 0.0263kg, and the pyrolysis gas of generation is about 0.6483kg.Percentage calculation by volume, the each component in the pyrolysis gas is: H
2-8.11%, CO
2-10.93%, CO-36.44%, H
2O-26.56%, CH
4-8.11%, N
2-1.39%, carbon two above organic components and other inorganic components-8.46%.
Embodiment three: raw material is changed to corn stalk.The corn stalk selection back of collecting is cleaned, removed earth and other impurity in the corn stalk.With raw material air-dry to material water ratio in 15～20% scope.Material after air-dry is packed in the cutting unit, and material is cut into the particle of particle diameter 5～80mm.The temperature of device of keeping dry is 120～140 ℃, and the residence time of material in moisture eliminator is 600～1000s.Keeping the temperature of asher is 300～500 ℃, and the residence time of material in charing rises is 400～800s.Learn that after testing to the charging of every 1kg corn stalk, the moisture content that moisture eliminator is discharged is about 0.052kg, the charcoal of generation is about 0.17kg, and ash is about 0.051kg, and the pyrolysis gas of generation is about 0.7337kg.Percentage calculation by volume, the each component in the pyrolysis gas is: H
2-9.96%, CO
2-8.05%, CO-26.83%, H
2O-33.86%, CH
4-9.97%, N
2-1.14%, carbon two above organic components and other inorganic components-10.19%.
The core of technology of the present invention is in the differing temps zone, earlier the biomass material deep dehydration is handled, and obtains biomass charcoal and pyrolysis gas by the high temperature carbonization reaction again.Equipment of the present invention organically is connected as a single entity moisture eliminator and asher, has realized the continuous processing and the Continuous Heat exchange of feed particles.Particularly by be provided with in asher bottom can the combustion parts material with provide the charing heat from thermic devices, and reverse Continuous Heat Transfer device is set on asher and drier enclosure, greatly improved the thermo-efficiency of entire equipment, both effectively reduced self-heating incendiary inventory, efficiently solve asher again and drive to enter the slow difficult problem of standard state, and improved CO, H in the gaseous product of carbonization reaction
2Content, thus realize technical object with the Wood Adhesives from Biomass high heating value volatile combustible burning pyrolysis gas that to be high-temperature gasification exist with the biomass charcoal of high-energy-density with gaseous form.Therefore, adopt technology of the present invention or moisture eliminator and asher shell to unite the structure of the equipment and the interior autothermal burner plate of asher of indirect reverse heat-exchange, all belong to protection scope of the present invention.
Claims (10)
1. biomass deep dehydration carbonization continuous processing technology, it mainly adopts outer thermal source successively continuously for the biomass material in asher and the moisture eliminator provides heat, and its technological process comprises the steps:
1) at first the biomass under the state of nature is chosen and cleared up, remove the waste material that dirt wherein, hard thing, impurity etc. do not meet production requirement, it is air-dry that the material of the selected suitable charing that goes out carries out routine, tentatively remove the external moisture content in the material, the water ratio of material is controlled in 15～20% the scope;
2) then the air-dry material of routine is carried out the machinery chopping and handle, the particle diameter of material particles is controlled in the scope of 5～80mm;
3) again the material particles of chopping is directly sent into and carried out deep dehydration in the moisture eliminator and handle, control the temperature of moisture eliminator in 120～160 ℃ scope by regulating outer thermal source, under the propulsive state of continuously stirring, the water ratio of material particles is reduced in 8～10% the scope;
4) at last the material particles of deep dehydration is sent into and carried out charing in the asher and handle, control the temperature of asher in 300～500 scope by regulating outer thermal source, under the propulsive state of continuously stirring, make material particles generation carbonization reaction, finally generate high-temperature gasification and burn pyrolysis gas with the biomass charcoal of high-energy-density with the high heating value volatile combustible that gaseous form exists.
2. biomass deep dehydration carbonization continuous processing technology according to claim 1, it is characterized in that: in the said step 4), make the spontaneous combustion of partial material particle or make the material particles temperature reduction way by adding the gaseous state auxiliary agent, the temperature that cooperates outer thermal source Collaborative Control asher is in 300～500 ℃ scope.
3. biomass deep dehydration carbonization continuous processing technology according to claim 1 and 2 is characterized in that: in the said step 3), it is 600～1200s that the stirring of material particles in moisture eliminator advances the residence time; In the said step 4), it is 200～1000s that the stirring of material particles in asher advances the reaction times.
4. biomass deep dehydration carbonization continuous processing technology according to claim 1 and 2 is characterized in that: the air pressure in said moisture eliminator and the asher all is controlled in the scope of 3.0～4.0MPa.
5. one kind is adopted the described technology of claim 1 and custom-designed biomass deep dehydration carbonization continuous processing apparatus, comprise moisture eliminator (6) and asher (12), moisture eliminator (6) has moisture eliminator material inlet (4), moisture eliminator screw feeder (17), moisture eliminator material outlet (7) and moisture eliminator steam outlet (9); Asher (12) has asher material inlet (10), asher stirring rake (25), asher coke export (13) and asher pyrolysis gas outlet (15); It is characterized in that:
The housing of moisture eliminator (6) is provided with the moisture eliminator interlayer heat exchange cavity (19) that passes through for outer thermal source medium, and the two ends of moisture eliminator interlayer heat exchange cavity (19) are respectively arranged with outer thermal source medium import (8) of moisture eliminator and the outer thermal source media outlet (5) of moisture eliminator;
The housing of asher (12) is provided with the asher interlayer heat exchange cavity (28) that passes through for outer thermal source medium, and the two ends of asher interlayer heat exchange cavity (28) are respectively arranged with outer thermal source medium import (14) of asher and the outer thermal source media outlet (11) of asher;
For sealing is connected, be to seal to be connected between the outer thermal source medium import (8) of moisture eliminator and the outer thermal source media outlet (11) of asher between moisture eliminator material outlet (7) and the asher material inlet (10).
6. biomass deep dehydration carbonization continuous processing apparatus according to claim 5 is characterized in that: outer thermal source medium import (8) of said moisture eliminator and the outer thermal source media outlet (5) of moisture eliminator are separately positioned on the side near moisture eliminator material outlet (7) and moisture eliminator material inlet (4); Outer thermal source medium import (14) of said asher and the outer thermal source media outlet (11) of asher are separately positioned on the side near asher coke export (13) and asher material inlet (10).
7. according to claim 5 or 6 described biomass deep dehydration carbonization continuous processing apparatus, it is characterized in that: the intracavity bottom of said asher (12) is provided with arc surfaced burner plate (23), be evenly equipped with gaseous state auxiliary agent nozzle (22) on the arc surfaced burner plate (23), gaseous state auxiliary agent nozzle (22) is connected with the gaseous state auxiliary agent inlet pipe of introducing from outside, asher (12) bottom (24).
8. biomass deep dehydration carbonization continuous processing apparatus according to claim 7, it is characterized in that: be formed with arc surfaced enclosed cavity (30) between said arc surfaced burner plate (23) and asher (12) bottom, said gaseous state auxiliary agent inlet pipe (24) is connected with gaseous state auxiliary agent nozzle (22) by arc surfaced enclosed cavity (30).
9. biomass deep dehydration carbonization continuous processing apparatus according to claim 7 is characterized in that: the arc angle of said arc surfaced burner plate (23) is designed to 70～110 °.
10. biomass deep dehydration carbonization continuous processing apparatus according to claim 7, it is characterized in that: said gaseous state auxiliary agent nozzle (22) is for calotte formula structure, and it is by nozzle pipe (31) and be installed in nozzle bubble-cap (32) formation of nozzle pipe (31) head.
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