CN100387367C - Biomass pyrolysis liquefied technique and apparatus system thereof - Google Patents
Biomass pyrolysis liquefied technique and apparatus system thereof Download PDFInfo
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- CN100387367C CN100387367C CNB2005100572162A CN200510057216A CN100387367C CN 100387367 C CN100387367 C CN 100387367C CN B2005100572162 A CNB2005100572162 A CN B2005100572162A CN 200510057216 A CN200510057216 A CN 200510057216A CN 100387367 C CN100387367 C CN 100387367C
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Abstract
The present invention relates to a biomass pyrolysis liquefying technical method and an apparatus system thereof. The technical method comprises the following steps that biomass materials are sent into a pyrolysis reaction tower so as to mix high-temperature fluidized gas and heat carriers with the powdery biomass materials and carry out thermal cracking for biomass, gas-solid separation is carried out for pyrolysis gas, carbon residue, etc. in a separator, the pyrolysis gas is condensed into biologic oil in a condenser, etc., wherein the heat carriers, the pyrolysis gas, the carbon residue, etc., are output from the pyrolysis reaction tower and sent into the system for circulation. Therefore, the apparatus system specially comprises a heat carrier separator by which the pyrolysis gas, the carbon residue, etc. are separated, and a heat carrier heater by which the separated heat carriers are heated. The present invention greatly increases the flow velocity of various materials in the system, further ensures a uniform and stable temperature field in the pyrolysis reaction tower, increases the heating rate, and shortens the stay time of gas phases. Since the adopted equipment or apparatus can be from the prior art, the apparatus system is suitable for industrialization application.
Description
Technical field
The present invention relates to the technical field of living beings regeneration and energy thereof, relate in particular to the process and the apparatus system thereof of biomass pyrolysis liquefaction.
Background technology
The energy is the basis that modern society depends on for existence and develops.More than 85% non-renewable fossil fuels such as coal, oil, natural gas in China's energy resource structure at present.These fossil fuels are not only deficient day by day, also environment caused serious pollution from exploiting in the systemic circulation that utilizes.Therefore, the clean energy resource of seeking reproducible utilization has become the problem that countries in the world all very are concerned about.Living beings (comprise various agricultural wastes, speed give birth to discarded object, water plant and the various organic wastes etc. of firewood carbon woods, forestry and wood processing industry) are exactly the raw material of the clean energy resource of the reproducible utilization that produces by photosynthesis.The biomass energy technology mainly comprises gasification, combustion power generation, solidification fuel and liquefaction etc.Gasification, combustion power generation, three kinds of technology of solidification fuel have reached the commercial level of comparative maturity.But from improving energy density, be convenient to store and the transportation equal angles, it is then ideal that biomass resource is converted to liquid (bio oil).And the bio oil of cleaning also has low ash, low-sulfur, produces the characteristics of pernicious gas hardly in combustion process; What is more important, the raw material of bio oil is living beings, can realize CO in the great circulation system of living beings utilization
2Zero-emission.The biomass liquefying technical matters can be divided into biochemical process and thermochemical method; Biochemical process mainly is meant by means such as hydrolysis or fermentations living beings is converted into alcohol fuel; Thermochemical method mainly comprises methods such as pressurized catalysis liquefaction and rapidly pyrolysing and liquefying.Biomass fast pyrogenation production bio oil technology is the most economic at present method that living beings is converted into liquid fuel.The process system formation of research biomass fast pyrogenation is identical basically both at home and abroad, forms by four major parts: the preparation of biomass material, fast pyrogenation, gas solid separation, rapid condensation.But the different units that research and develop adopt the pyrolysis way and different carrier mode of heatings that is not quite similar, and have determined that there is bigger difference in the biomass liquefying technology path.Application for a patent for invention number is that 03128901.0 " technology of low energy consumption biomass through pyrolysis and device thereof " is exactly a kind of process system of pyrolysis liquefaction living beings.Definite device comprises dispenser, fluidized-bed reactor, cyclone separator, the gas～gas-heat exchanger as energy recovery, gas～water heat exchanger, oil catcher, Roots's circulating fan, main electric heater, the electrical auxiliary heater of being made up of frequency modulation motor, charging rod, hopper by the thermal cracking process flow process of this application case proposition; Fluidized-bed reactor is vertically placed, and the bottom is equipped with porous plate, and puts into quartz sand as intermediate carrier; Main electric heater places the reactor inlet front end, and electrical auxiliary heater places the reactor outside wall surface.Key equipment wherein is fluidized-bed reactor (corresponding with this case " pyrolytic reaction tower ").From the disclosed content of this application case, the purpose of its invention is to have reached.But thermal cracking process flow process that this application case is disclosed and device thereof only are suitable for the mechanism Journal of Sex Research, will be restricted in industrial applications.Because the intermediate carrier of this application case (this case claims " thermophore ", also can claim " heat carrier ") is retained in the fluidized-bed reactor in whole process flow all the time.And in order to satisfy the requirement of this technological process, it enters high temperature nitrogen (this case claims " fluidized gas ") in the fluidized-bed reactor and sends the dynamic pressure value (unit head) of fluidized-bed reactor gasified bio-matter (this case claims " pyrolysis gas ") outward all can not be big, otherwise the solid matter that carrier also can stay after gasified bio-matter and pyrolysis thereof in the middle of it is sent in the cyclone separator and goes.Like this, not only do not reach goal of the invention, also can force whole thermal cracking processes to stop when serious.Therefore, the thermal cracking speed of this application case is not high, can only be used for the mechanism Journal of Sex Research of biomass through pyrolysis.
Summary of the invention
The objective of the invention is at the deficiencies in the prior art, propose a kind of thermal cracking speed height, can be used for the process and the apparatus system thereof of the biomass pyrolysis liquefaction of suitability for industrialized production.
What realize described goal of the invention is a kind of like this process of biomass pyrolysis liquefaction, it comprises by feed mechanism sends into biological material step in the pyrolytic reaction tower, allows high-temperature stream gasification and heating medium for high temperature mix with biological material living beings are carried out the step of thermal cracking in the pyrolytic reaction tower, in separator, pyrolysis gas and carbon residue and ash are carried out the step of gas solid separation, and in condenser the congeal into step of bio oil of pyrolysis air cooling.Fluidized gas wherein is thermally-stabilised fabulous, the inert gas or the nitrogen that can not cause oxidation reaction itself, and this case is the same with prior art, selects for use nitrogen as fluidized gas; Thermophore also is that itself is thermally-stabilised fabulous and be difficult for the particulate matter of powdered, and it can be the river sand etc. that satisfies performance requirement, also can just directly adopt quartz sand, and this case is the same with prior art, also selects quartz sand for use.In the pyrolytic reaction tower, high-temperature stream gasification and heating medium for high temperature can very rapidly make its thermal cracking apace to the heat transferred living beings with after living beings are fully mixed.Difference with the prior art part of the present invention is the further comprising the steps of and condition of this process:
A, before thermal cracking is carried out in feeding, biological material is dried to moisture content less than 8%, pulverize and to make the step of particle diameter less than the living beings powder of 2mm;
Pressure in b, the pyrolytic reaction tower is 0.08～0.12MPa, and temperature range is 400～570 ℃, and the heating rate of living beings powder in the pyrolytic reaction tower is 500～1000 ℃/s; The living beings powder is sent in the step in the pyrolytic reaction tower by feed mechanism, be attended by the circulation carrier gas living beings powder in the feed mechanism is assisted the process of carrying (the so-called carrier gas in this case has been meant the gas of circulation conveying effect, include nitrogen in the carrier gas and hereinafter with the incondensable gas of mentioning);
C, living beings powder carry out the step end of thermal cracking in the pyrolytic reaction tower after, its thermophore is sent (obviously in the pyrolytic reaction tower with pyrolysis gas, carbon residue and ash, be mixed with carrier gas in the said herein pyrolysis gas of this case, and the temperature of contained nitrogen is lower many during as fluidized gas than it in the carrier gas).Then, there is one thermophore and pyrolysis gas, carbon residue and ash separation steps;
D, when the pyrolysis gas of separating and carbon residue and ash enter the gas solid separation step, the thermophore of separating enters one and preheats step, certainly, its pre-heating temperature is to come requirement according to the heating rate of different living beings powders in the pyrolytic reaction tower, heating rate is fast, and its pre-heating temperature requires high; Otherwise, low spot then.Usually, the thermophore temperature after preheating is controlled between 550～750 ℃; Then, there is one the thermophore after the preheating sent in the pyrolytic reaction tower for the step that recycles again; Entering the interior thermophore of pyrolytic reaction tower and the quality ratio of living beings powder is 1.8～4.6;
E, enter the step that is condensed into bio oil from the isolated pyrolysis gas of gas solid separation step; In condenser, pyrolysis gas is with the speed cooling of 400～800 ℃/s; Incondensable gas and with the defeated carrier gas that comes of pyrolysis gas in condenser with after the bio oil of condensation is separated, collect as reclaiming gas;
F, recovery gas mix with the nitrogen that replenishes; Mixed gas is defeated before dividing two-way to continue, and the flow ratio of two-way is 5.5～6.5; Ratio less a road as the circulation carrier gas send in the described feed mechanism once more, so that the living beings powder is assisted conveying; Becoming fluidized gas after one tunnel heating of large percentage is input in the pyrolytic reaction tower once more.Obviously, the said fluidized gas of this case under recycling situation, has just comprised incondensable gas except that being the high temperature nitrogen in this fluidized gas when using for the first time.
The apparatus system of realizing the process of this biomass pyrolysis liquefaction comprises: the interior carrier gas input pipe of feeding device, feed mechanism and access feed mechanism that performing step b is used; The living beings powder is carried out the pyrolytic reaction tower of thermal cracking, and this pyrolytic reaction tower is vertically placed, and the bottom is provided with the wind distributing hole plate; The thermophore separator that thermophore and pyrolysis gas, carbon residue and ash are separated and to the thermophore heater of isolated thermophore heating; The gas-solid separator that pyrolysis gas and carbon residue and ash are separated; Condensation goes out the condenser and the oil catcher thereof of bio oil from pyrolysis gas, collects the air accumulator and the air pump thereof that reclaim gas; The nitrogen pot that its outlet is in parallel with the outlet of air accumulator; The fluidized gas heater that fluidized gas is heated; And the pipeline of connection said apparatus and corresponding control valve, Pressure gauge and the thermometer on pipeline.
Be not difficult to find out that from scheme except that the small part thermal lift, the periodic duty power of native system mainly comes from gas pump.Obviously, the supply gas pressure of this gas pump and flow can be regulated.
Compared with prior art, the present invention has following progress:
1, because before thermal cracking is carried out in feeding, biological material is dried to moisture content less than 8%, pulverizes and to make particle diameter less than the living beings powder of 2mm, so, when in the pyrolytic reaction tower, carrying out thermal cracking, needn't wasted heat remove the moisture in the dried biomass material.Like this, thermal cracking efficient has just had raising naturally;
2, send from the pyrolytic reaction tower with pyrolysis gas, carbon residue and ash owing to thermophore, so, just needn't as prior art, go painstakingly to reduce speed that their flow.Because the raising of flowing velocity, and then the living beings powder is mixed fully with thermophore, fluidized gas.Like this, just really guaranteed that the temperature field is uniform and stable, the rate of heat addition improves, and the gas phase time of staying shortens---just can be fit to industrial applications;
3, because thermophore is to heat at independent thermophore heater, so, to the adjusting of its heating-up temperature, the rate of heat addition also than the convenience of prior art, more help control in industrial applications;
4, in the process of recycling carrier gas (particularly including wherein contained heat), can replenish nitrogen in time, more continuous suitability for industrialized production has been created condition.
It can also be seen that from process of the present invention that 5, selected equipment or device all can be selected for use existing.For example: pyrolytic reaction tower wherein is exactly that to have utilized the fluidization of comparative maturity and reaction tower thereof, gas pump can be exactly Roots's circulating fan.Therefore, the present invention is simple in structure in addition, and the equipment investment expense is hanged down this advantage.
The present invention is further illustrated below in conjunction with accompanying drawing.
Description of drawings
Fig. 1---(filled arrows among the figure is in this circulatory system to the apparatus system schematic diagram of application process of the present invention, the flow direction of each related substances; Dotted arrow among the figure is the cooling-water flow direction)
Wherein: the 1-feeding device; The 2-adjustable frequency motor; The 3-helix transporting device; The 4-feed pipe; The 5-cooling jacket; 6-wind distributing hole plate; 7-pyrolytic reaction tower; 8-thermophore separator; 9-thermophore heater; 10-thermophore adjuster; 11-thermophore circulation pipe; The 12-gas-solid separator; The 13-condenser; The 14-oil catcher; The 15-pneumatic filter; The 16-gas pump; The 17-air accumulator; The 18-nitrogen pot; 19-fluidized gas heater; 20-fluidized gas control valve; 21-carrier gas control valve.
The specific embodiment (all in conjunction with Fig. 1)
In view of can adopting existing equipment or device, apparatus of the present invention system forms; Simultaneously, also systematically understand the present invention for convenience of those skilled in the art.In this specific embodiment, the apparatus system of process and this method of realization is combined disclosure in the lump.
A kind of process of biomass pyrolysis liquefaction and apparatus system thereof.By following processing step, in following apparatus system, realize:
A, before thermal cracking is carried out in feeding, carry out the preliminary treatment (only this step is outside this apparatus system) of material, biological material is dried to moisture content less than 8%, pulverize and make the living beings powder of particle diameter less than 2mm.
B, pour in the feeding device 1 the living beings powder into storage.This feeding device 1 and feed mechanism UNICOM are inserted with the delivery cycle carrier gas with the auxiliary carrier gas input pipe of carrying the living beings powder in this feed mechanism.Under the acting in conjunction of feed mechanism and circulation carrier gas, in the living beings powder is imported into this reaction tower from the bottom of pyrolytic reaction tower 7.Also be connected with a thermophore circulation pipe 11 in the bottom of this pyrolytic reaction tower 7, thermophore (quartz sand after preheated) is imported in the pyrolytic reaction tower 7 by this circulation pipe, and entering the thermophore in the pyrolytic reaction tower 7 and the quality ratio of living beings powder is 1.8～4.6.Be connected with the fluidized gas input pipe in the bottom of pyrolytic reaction tower 7, (when using for the first time, be the nitrogen after preheating, and utilize the air in this nitrogen emptying apparatus system by this input pipe, fluidized gas; After recycling, be the nitrogen after preheating and the gaseous mixture of noncondensing gas) be transfused in this pyrolytic reaction tower 7.Pressure in the pyrolytic reaction tower 7 is 0.08～0.12MPa, and temperature range is 400～570 ℃, and the heating rate of living beings powder in pyrolytic reaction tower 7 is controlled between 500～1000 ℃/s;
C, living beings powder carry out the step end of thermal cracking in pyrolytic reaction tower 7 after, its thermophore is exported from the top of pyrolytic reaction tower 7 with pyrolysis gas, carbon residue, ash, pass through pipeline, enter in this separator from the top of a centrifugal thermophore separator 8, thermophore separates in this separator with pyrolysis gas, carbon residue, ash;
D, the pyrolysis gas of separating and carbon residue and ash be from the output of the top of thermophore separator 8, by pipeline, enters in this separator from the top of a centrifugal gas-solid separator 12.From these gas-solid separator 12 isolated carbon residue and ash, to discharge from the bottom of this separator, pyrolysis gas is sent in the condenser 13 by pipeline from the top of this separator.
The technical process of gas solid separation process another route arranged side by side (just with) simultaneously, the thermophore of from thermophore separator 8, separating, directly be admitted to the thermophore heater 9 preheatedly from the bottom of this separator, its pre-heating temperature is 550～750 ℃.The other end that is connected the thermophore circulation pipe 11 of pyrolytic reaction tower 7 bottoms is connected the bottom of this thermophore heater 9, and a thermophore adjuster 10 (or perhaps the Flow-rate adjustment of thermophore, gauge tap) is installed in the junction of this thermophore circulation pipe 11 and thermophore heater 9.Thermophore after the preheating is admitted in the pyrolytic reaction tower 7 for recycling (when using for the first time, being earlier thermophore to be put into this thermophore heater 9 to carry out pre-warmed) by this thermophore circulation pipe 11 again.By the adjusting of thermophore adjuster 10, be controlled between 1.8～4.6 entering the thermophore in the pyrolytic reaction tower 7 and the quality ratio of living beings powder;
E, the waist from the isolated pyrolysis gas of gas solid separation step from condenser 13 enter condenser 13, and the heat exchange medium of condenser 13 is a water.In condenser 13, pyrolysis gas is cooled with the speed of 400～800 ℃/s.Incondensable gas and with the defeated carrier gas that comes of pyrolysis gas in condenser 13 with after the bio oil of condensation is separated, become and reclaim the top output of gas from condenser 13.The bio oil of condensing is exported from the bottom of this condenser 13, enters in the oil catcher 14 to collect;
The recovery gas delivery outlet at f, condenser 13 tops and one are fitted with between safety valve and the manometric air accumulator 17 and are connected with appendix, on this appendix, pneumatic filter 15 and a gas pump 16 are installed by the gas transmission order, reclaim gas under the effect of gas pump 16, in appendix, enter temporary transient storage the in the air accumulator 17 by pneumatic filter 15 and gas pump 16.
A nitrogen pot 18 that its outlet is in parallel with the outlet of this air accumulator 17 is arranged.Store in this nitrogen pot 18 for first and use and the sufficient nitrogen of usefulness as a supplement during periodic duty.Air accumulator 17 and nitrogen pot 18 exit in parallel has the pipeline of two parallel connections again again to the last period.Article one, pipeline is connected to the bottom of pyrolytic reaction tower 7, as the fluidized gas input pipe.Order is equipped with fluidized gas heater 19 and fluidized gas control valve 20, thermometer that also is necessary and Pressure gauge on this fluidized gas input pipe.Another pipeline is exactly the auxiliary carrier gas input pipe of carrying the living beings powder, at this carrier gas input pipe carrier gas control valve 21 and Pressure gauge is installed.Reclaim gas and nitrogen at air accumulator 17 with after mix in the exit of nitrogen pot 18 parallel connections, by the adjusting of fluidized gas control valve 20 and carrier gas control valve 21, be 5.5～6.5 preceding the failing of relation continuation according to the ratio of fluidized gas and carrier gas.Wherein, after fluidized gas preheats by fluidized gas heater 19, enter next working cycles in the input pyrolytic reaction tower 7; Carrier gas then directly imports in the feed mechanism, so that the living beings powder is assisted conveying, also enter next working cycles.
The same as known for those skilled in the art, in this specific embodiment, need must wrap up insulation material on the unit or pipeline of parcel insulation material.It will be apparent to those skilled in that native system also comprises various instruments, the instrument that monitors or observe running status certainly, the various valves of control running status etc.Do not give unnecessary details at this.
The description of above the specific embodiment is following each routine summation, and in following each example, the content identical with this part summation do not given unnecessary details yet.
Embodiment 1:
This example is on the basis of summation part, carries the mode of thermophore or further specializing of structure at thermophore circulation pipe 11 wherein.That is: in this routine apparatus system, the outlet of thermophore heater 9 output thermophores is higher than the import that pyrolytic reaction tower 7 is input into this thermophore, the thermophore circulation pipe 11 that connects this outlet and this import tilts, and the angle of its incline direction and horizontal plane is greater than 45 °.That is to say, in this example, be to rely on the gravity of the thermophore self after preheated to carry.Like this, just further saved the operating cost of system.Obviously, if each concrete device itself and place allow, the incline direction of this thermophore circulation pipe 11 and the angle of horizontal plane can also be bigger, and this thermophore circulation pipe 11 can also be steeper in other words.
Embodiment 2:
This example is on the basis of summation part or embodiment 1, at wherein with carrier gas the living beings powder assist the further specific of mode of movement or structure.That is: in this routine apparatus system, feed mechanism comprises the feed pipe 4 of helix transporting device 3 and outlet that is connected this helix transporting device 3 and 7 imports of pyrolytic reaction tower.This helix transporting device 3 is driven by a frequency conversion motors 2.The version that inserts carrier gas input pipe in the feed mechanism and be with injector taps in its feed pipe 4.Waist at this carrier gas input pipe also has a branched pipe (with dashed lines draws in the accompanying drawing), and the outlet of this branched pipe taps in the feeding device 1, on the charge door of this feeding device 1 seal cover is arranged.That is to say, this example can combine the rotational speed regulation (transporting velocity of decision helix transporting device 3) of the aperture of thermophore adjuster 10 being regulated with to adjustable frequency motor 2, according to different biomass materials and the thermal cracking situation in pyrolytic reaction tower 7 thereof, the mass ratio of thermophore of Tiao Jieing and living beings powder exactly.Obviously, this example is applicable to that carrier gas dynamic pressure in the carrier gas input pipe is unlike the high situation of pressure in the pyrolytic reaction tower 7.
Embodiment 3:
This example is substantially the same manner as Example 2, promptly remains the feed pipe 4 that feed mechanism comprises helix transporting device 3 and outlet that is connected this helix transporting device 3 and 7 imports of pyrolytic reaction tower.This helix transporting device 3 is driven by a frequency conversion motors 2.The version that inserts carrier gas input pipe in the feed mechanism and be with injector taps in its feed pipe 4.Different is that the dynamic pressure of carrier gas is greater than the static pressure of pyrolytic reaction tower 7 import departments, to allow carrier gas with the mode of entrainmenting the living beings powder be assisted conveying (because the version those skilled in the art of injector is clearly, so do not draw the local cutaway view that amplifies separately).In other words, the dynamic pressure that allows to reach carrier gas when the whole system operation situation is during greater than the static pressure of pyrolytic reaction tower 7 import departments, just can not adopt among the embodiment 2 branched pipe and add the structure of seal cover.Obviously, the apparatus system that embodiment 2 is disclosed also goes for the situation of the dynamic pressure of its carrier gas greater than pyrolytic reaction tower 7 import department's static pressure, in the case, stop up or close that branched pipe that enters in the feeding device 1 and get final product, its seal cover also can cover completely.Like this, just the same with this example, be more suitable for continuity ground production bio oil.
If desired, in the apparatus system of embodiment 2 or embodiment 3, increase in can feeding device 1 therein an agitator is set.For example, for carrying the living beings powder that particle diameter is less and adhesiveness is stronger, just can make them successfully drop into helix transporting device 3 down by stirring and suffer.
Embodiment 4:
This example is on the basis of embodiment 2 or embodiment 3, at the further improvement of wherein feed pipe 4 structures.Its improved aspect is that feed pipe 4 is wrapped with cooling jacket 5.Like this, make with regard to having stopped contingent heat affecting up hill and dale that some living beings powder is bonded on the tube wall of this feed pipe 4, the situation of caking near the feed pipe 4 of pyrolytic reaction tower 7 import departments even owing to pyrolytic reaction tower 7.
Following table is the part test data of embodiment 4:
Other tests confirm (those skilled in the art also can normally analyze, inference draw): the living beings of other raw materials of powder particle diameter＜2mm also condensation normally in the present invention go out bio oil---liquefied fraction difference just.
Equally, after seeing the disclosed scheme of this specification that is over, the specific embodiment and " part test data " thereof, those skilled in the art is only by conventional analysis, inference, with regard to the same approval concrete parameter area that this case proposed---and different just efficient height and/or energy loss-rates have certain difference.
Claims (7)
1. the process of a biomass pyrolysis liquefaction, it comprises by feed mechanism sends into biological material the interior step of pyrolytic reaction tower (7), allows high-temperature stream gasification and heating medium for high temperature mix with biological material living beings are carried out the step of thermal cracking in pyrolytic reaction tower (7), in separator, pyrolysis gas and carbon residue and ash are carried out the step of gas solid separation, and in condenser (13) the congeal into step of bio oil of pyrolysis air cooling; It is characterized in that the further comprising the steps of and condition of this process:
A, before thermal cracking is carried out in feeding, biological material is dried to moisture content less than 8%, pulverize and to make the step of particle diameter less than the living beings powder of 2mm;
Pressure in b, the pyrolytic reaction tower (7) is 0.08～0.12MPa, and temperature range is 400～570 ℃, and the heating rate of living beings powder in pyrolytic reaction tower (7) is 500～1000 ℃/s; The living beings powder is sent in the interior step of pyrolytic reaction tower (7) by feed mechanism, be attended by the circulation carrier gas and the living beings powder in the feed mechanism assisted the process of carrying;
C, living beings powder carry out the step end of thermal cracking in pyrolytic reaction tower (7) after, its thermophore is sent in pyrolytic reaction tower (7) with pyrolysis gas, carbon residue and ash; Then, there is one thermophore and pyrolysis gas, carbon residue and ash separation steps;
D, when the pyrolysis gas of separating and carbon residue and ash enter the gas solid separation step, the thermophore of separating enters one and preheats step; Then, there is one the thermophore after the preheating sent in the pyrolytic reaction tower (7) for the step that recycles again; Entering the interior thermophore of pyrolytic reaction tower (7) and the quality ratio of living beings powder is 1.8～4.6;
E, enter the step that is condensed into bio oil from the isolated pyrolysis gas of gas solid separation step; In condenser (13), pyrolysis gas is with the speed cooling of 400～800 ℃/s; Incondensable gas and with the defeated carrier gas that comes of pyrolysis gas in condenser (13) with after the bio oil of condensation is separated, collect as reclaiming gas;
F, recovery gas mix with the nitrogen that replenishes; Mixed gas is defeated before dividing two-way to continue, and the two-way flow ratio is 5.5～6.5; Ratio less a road as the circulation carrier gas send in the described feed mechanism once more, so that the living beings powder is assisted conveying; Becoming fluidized gas after one tunnel heating of large percentage is input in the pyrolytic reaction tower (7) once more.
2. realize the apparatus system of the process of the described a kind of biomass pyrolysis liquefaction of claim 1, it is characterized in that this apparatus system comprises: the interior carrier gas input pipe of feeding device (1), feed mechanism and access feed mechanism that performing step b is used; The living beings powder is carried out the pyrolytic reaction tower (7) of thermal cracking, and this pyrolytic reaction tower (7) is vertically placed, and the bottom is provided with wind distributing hole plate (6); The thermophore separator (8) that thermophore and pyrolysis gas, carbon residue and ash are separated and to the thermophore heater (9) of isolated thermophore heating; The gas-solid separator (12) that pyrolysis gas and carbon residue and ash are separated; Condensation goes out the condenser (13) and the oil catcher (14) thereof of bio oil from pyrolysis gas, collects the air accumulator (17) and the air pump thereof that reclaim gas; The nitrogen pot (18) that its outlet is in parallel with the outlet of air accumulator (17); The fluidized gas heater (19) that fluidized gas is heated; And the pipeline of connection said apparatus and corresponding control valve, Pressure gauge and the thermometer on pipeline.
3. the apparatus system of the process of a kind of biomass pyrolysis liquefaction of realization according to claim 2, it is characterized in that, the outlet of described thermophore heater (9) output thermophore is higher than the import that pyrolytic reaction tower (7) is input into this thermophore, what connect this outlet and this import is a thermophore circulation pipe (11), this thermophore circulation pipe (11) tilts, and the angle of its incline direction and horizontal plane is greater than 45 °.
4. according to the apparatus system of the process of claim 2 or a kind of biomass pyrolysis liquefaction of 3 described realizations, it is characterized in that, described feed mechanism comprises the feed pipe (4) of helix transporting device (3) and outlet that is connected this helix transporting device (3) and pyrolytic reaction tower (7) import, and the version that inserts carrier gas input pipe in the feed mechanism and be with injector taps in its feed pipe (4); Waist at this carrier gas input pipe has a branched pipe, and the outlet of this branched pipe taps in the described feeding device (1), on the charge door of this feeding device (1) seal cover is arranged.
5. according to the apparatus system of the process of claim 2 or a kind of biomass pyrolysis liquefaction of 3 described realizations, it is characterized in that, described feed mechanism comprises the feed pipe (4) of helix transporting device (3) and outlet that is connected this helix transporting device (3) and pyrolytic reaction tower (7) import, the version that inserts carrier gas input pipe in the feed mechanism and be with injector taps in its feed pipe (4), and the dynamic pressure of carrier gas is greater than the static pressure of pyrolytic reaction tower (7) import department, to allow carrier gas with the mode of entrainmenting the living beings powder be assisted conveying.
6. the apparatus system of the process of a kind of biomass pyrolysis liquefaction of realization according to claim 4 is characterized in that, is wrapped with cooling jacket (5) at described feed pipe (4).
7. the apparatus system of the process of a kind of biomass pyrolysis liquefaction of realization according to claim 5 is characterized in that, is wrapped with cooling jacket (5) at described feed pipe (4).
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| CN100554377C (en) * | 2007-02-13 | 2009-10-28 | 中国矿业大学 | The method and apparatus of a kind of biomass liquefied oil under mild condition modification, upgrading |
| CN101016467B (en) * | 2007-02-13 | 2010-11-03 | 安徽易能生物能源有限公司 | Comprehensive utilization method of product of biomass pyrolysis liquefaction process |
| CN101285002B (en) * | 2008-05-06 | 2011-08-24 | 中国科学技术大学 | Process for separating bio-oil via solvent with high boiling point |
| CN101613617B (en) * | 2009-07-23 | 2012-07-04 | 东南大学 | Method for preparing biological oil through vacuum pyrolysis of biomasses |
| CN101974346A (en) * | 2010-10-29 | 2011-02-16 | 广州迪森热能技术股份有限公司 | Preparation method of ecological oil |
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