CN100360248C - Biomass pyrolysis liquefied technique and double tower apparatus system thereof - Google Patents
Biomass pyrolysis liquefied technique and double tower apparatus system thereof Download PDFInfo
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- CN100360248C CN100360248C CNB2005100572158A CN200510057215A CN100360248C CN 100360248 C CN100360248 C CN 100360248C CN B2005100572158 A CNB2005100572158 A CN B2005100572158A CN 200510057215 A CN200510057215 A CN 200510057215A CN 100360248 C CN100360248 C CN 100360248C
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Abstract
The present invention relates to a biomass pyrolysis liquefying technical method and a two-tower type apparatus system thereof. The technical method comprises the steps that biomass is sent into a pyrolysis reaction tower to be mixed with high-temperature fluidized gas and high-temperature heating carriers so as to carry out thermal cracking for the biomass; gas-solid separation is carried out for pyrolysis gas, carbon residue and ash in a separator, the pyrolysis gas is condensed into biologic oil in a condenser, etc., wherein the heating carriers, the pyrolysis gas, the carbon residue, etc., are output into a circulation system from the circulation system, and the carbon residue is used for preheating the heating carriers. Therefore, the two-tower type apparatus system of the present invention is especially provided with a primary separator for separating the heating carrier from the carbon residue and other substances for one time, and a heating carrier heating tower for burning the carbon residue. The present invention ensures a uniform and stable temperature field in the pyrolysis reaction tower due to the increased circulation velocity, the heating rate is increased, and the stay time of gas phases are shortened. Since the present invention can utilize the existing apparatus and use the carbon residue as heat sources, the present invention really adapts to industrialization and protects environment.
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 the zero-emission of CO2 in the great circulation system of living beings utilization.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 (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.Further, this application case is " ... hot cracked back generates fluid, gas, three kinds of products of solid ", just except that bio oil, also has accessory substance---noncondensing gas and carbon residue.Like this,, will increase the container of collecting them, also will seek really can utilize their approach if utilize the latter; If abandon them, the operating cost of then extracting bio oil is just higher.Therefore, this application case 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, a kind of speed height that extracts bio oil is proposed, especially in extracting the process of bio oil, self can utilize noncondensing gas and carbon residue and reduce the process and the apparatus system thereof of utilization biomass pyrolysis liquefaction cost, that can be used for 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, 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 carbon residue and pyrolysis gas and ash separation steps;
D, in the step of described gas solid separation, be that pyrolysis gas separates with ash; When entering the gas solid separation step, thermophore of separating suddenly in previous step and carbon residue enters a burning carbon residue, to preheat the step of thermophore;
E, preheat thermophore after, enter a step that this thermophore and waste gas and ash are separated;
F, the thermophore of separating enter one it are carried out the step of temperature adjustment, and certainly, the thermophore temperature after the temperature adjustment is to come requirement according to the heating rate of different living beings powders in the pyrolytic reaction tower, and heating rate is fast, and the temperature requirement of thermophore is high; Otherwise, low spot then.Usually, the thermophore temperature after the temperature adjustment is controlled between 550～750 ℃; Then, there is one the thermophore after the temperature adjustment 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; Simultaneously, there is the heat of waste gas that a utilization separates and ash to preheat the step of combustion air; Combustion air after preheated is admitted to the described burning carbon residue of steps d, preheat carry out in the step of thermophore combustion-supporting;
G, after the gas solid separation described in the d step is finished, isolated pyrolysis gas enters the step that is condensed into bio oil; 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;
H, recovery gas mix with the nitrogen that replenishes; Defeated before mixed gas divides three the tunnel to continue, one road band that contained incondensable gas enters described burning carbon residue in this recovery gas, preheat in the step of thermophore and burn with carbon residue; Two-way is pressed flow ratio 5.5～6.5 distribution more in addition; 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; A road of large percentage is input in the pyrolytic reaction tower once more as fluidized gas.
Realize this biomass pyrolysis liquefaction process be a kind of double tower apparatus system, this apparatus system comprises: the carrier gas input pipe in used feeding device, feed mechanism and the access feed mechanism of performing step b; 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 initial separator that thermophore and carbon residue and pyrolysis gas and ash are separated; Burn within it carbon residue, with the thermophore heating tower that preheats thermophore and the thermophore carbon residue circulation pipe of this thermophore heating tower of UNICOM and initial separator thereof; The thermophore separator that thermophore after this heating and waste gas and ash are separated; The thermophore of separating is carried out the thermophore thermosistor of temperature adjustment and the thermophore after the temperature adjustment is imported thermophore loopback pipe in the pyrolytic reaction tower into; Allow heat exchanger that the high-temp waste gas separated and ash preheat combustion air and the air blast of carrying combustion air; The gas-solid separator that pyrolysis gas 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 gas pump thereof that reclaim gas; The nitrogen pot that its outlet is in parallel with the outlet of air accumulator; And the pipeline of connection said apparatus and corresponding control valve, Pressure gauge and the thermometer on pipeline.
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 carry out pre-warmedly in independent carrier heating tower, that is to say in the pyrolytic reaction tower and only living beings are carried out thermal cracking.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; Especially carrying out in the carrier heating tower the pre-warmed fuel of thermophore is to hesitate to discard, recycle carbon residue and the incondensable gas that some other new problem is arranged again in the prior art.Like this, not only greatly reduce system's (production bio oil) operating cost, and, also realized energy-saving and cost-reducing and to the protection of ecological environment from recycling resource aspect.
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.This also is to be fit to the condition that industrial applications is possessed.
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-adjustable frequency motor; The 2-feeding device; The 3-helix transporting device; 4-pyrolytic reaction tower; 5-thermophore separator; 6-thermophore heating tower; The 7-air blast; The 8-heat exchanger; The 9-initial separator; The 10-gas-solid separator; The 11-condenser; The 12-pneumatic filter; The 13-oil catcher; The 14-gas pump; The 15-air accumulator; The 16-nitrogen pot; 17-thermophore thermosistor; 18-fluidized gas thermosistor; The 19-feed pipe; The 20-cooling jacket; 21-carrier gas control valve; 41-wind distributing hole plate; 42-fluidized gas control valve; 417-thermophore loopback pipe; 51-thermophore adjuster; 69-thermophore carbon residue circulation pipe.
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.
The process of biomass pyrolysis liquefaction and double tower apparatus system thereof.Realize by following processing step and in following double tower apparatus system:
A, (only this step is outside this apparatus system to carry out the preliminary treatment of material before thermal cracking is carried out in feeding; Also can utilize the waste heat of the waste gas that system discharges and in native system, increase drying device again), 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 2 the living beings powder into storage.This feeding device 2 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 4.Also be connected with a thermophore loopback pipe 417 in the bottom of this pyrolytic reaction tower 4, thermophore (quartz sand after preheated) is imported in the pyrolytic reaction tower 4 by this circulation pipe, and entering the thermophore in the pyrolytic reaction tower 4 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 4, (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 4.Pressure in the pyrolytic reaction tower 4 is 0.08～0.12MPa, and temperature range is 400～570 ℃, and the heating rate of living beings powder in pyrolytic reaction tower 4 is controlled between 500～1000 ℃/s;
C, living beings powder carry out the step end of thermal cracking in pyrolytic reaction tower 4 after, its thermophore is with the top output from pyrolytic reaction tower 4 of pyrolysis gas, carbon residue and ash, pass through pipeline, enter in this separator 9 from the top of a centrifugal initial separator 9, thermophore separates in this initial separator 9 with ash with pyrolysis gas with carbon residue;
D, the pyrolysis gas of separating from initial separator 9 and ash (obviously, contain the carbon residue with the suitable fine-powdered of their proportion in this ash) export from the top of this initial separator 9, enter this separator 10 to carry out gas solid separation from the top of gas-solid separator 10; Meanwhile, suddenly thermophore of separating from previous step and carbon residue are transfused to from the bottom of this initial separator 9, by a thermophore carbon residue circulation pipe 69, from a thermophore heating tower's 6 bottom in this heating tower 6, enter a burning carbon residue, to preheat the step of thermophore.Be connected with two input pipes in this thermophore heating tower 6 bottom, article one, input pipe in this heating tower 6, import reclaim gas (contain flammable noncondensing gas, this noncondensing gas also in thermophore heating tower 6 internal combustion, to preheat thermophore) and the additional nitrogen of part; Article one, input pipe is imported the combustion air through being heated behind the heat exchanger 8 in this heating tower 6, and this combustion air is provided by air blast 7.Obviously, the input quantity of this combustion air can carry out degree of being to guarantee oxygen debt burning.When this apparatus system of initial start-up, charge into nitrogen earlier with the intrasystem air of emptying, then, send into the living beings powder to thermophore heating tower 6 in right amount, light powder with a small amount of combustion gas, last, a gas pump 14 in the open system is so that this intrasystem gas enters the periodic duty state;
E, preheat in the process of thermophore, thermal lift by pressure that reclaims gas, combustion air and the generation of burning back, progressively the top output of the thermophore after preheating from this thermophore heating tower 6, by pipeline, from this separator 5 is sent into on the top of a thermophore separator 5, to enter a step that this thermophore and waste gas and ash are separated.Isolated waste gas and the ash that has heat enters heat exchanger 8 so that described combustion air is heated, waste gas after its heat is fully utilized and ash are discharged from the outlet of heat exchanger 8, it is pending or do him in addition with (for example to collect the back, after ash separation wherein, waste gas is inserted in the drying device, utilize its waste heat to come the dried biomass raw material);
F, the thermophore separated from thermophore separator 5 enter into described thermophore loopback pipe 417 from the bottom of this separator 5, a thermophore thermosistor 17 that thermophore in managing is carried out temperature adjustment is arranged outside thermophore loopback pipe 417, and the thermophore temperature after the temperature adjustment is controlled between 550～750 ℃; Then, the thermophore after the temperature adjustment is sent in the pyrolytic reaction tower 4 for recycling again.A thermophore adjuster 51 (or perhaps the Flow-rate adjustment of thermophore, gauge tap) is installed in this thermophore loopback pipe 417 and thermophore heating tower's 6 junction, by the adjusting of thermophore adjuster 51, control the thermophore that enters in the pyrolytic reaction tower 4 and the quality ratio of living beings powder;
G, after the gas solid separation described in the d step is finished, isolated ash is discharged from the bottom of this gas-solid separator 10 and is collected; Isolated pyrolysis gas is from the output of the top of gas-solid separator 10, enter condenser 11 from the waist of condenser 11, and the heat exchange medium of condenser 11 is a water.In condenser 11, pyrolysis gas is cooled with the speed of 400～800 ℃/s.The bio oil of condensing is exported from the bottom of this condenser 11, enters in the oil catcher 13 to collect; Incondensable gas and with the defeated carrier gas that comes of pyrolysis gas in condenser 11 with after the bio oil of condensation is separated, as reclaiming the top output of gas from condenser 11.The recovery gas delivery outlet at these condenser 11 tops and one are fitted with between safety valve and the manometric air accumulator 15 and are connected with appendix, on this appendix, pneumatic filter 12 and described gas pump 14 are installed by the gas transmission order, reclaim gas under the effect of gas pump 14, in appendix, enter temporary transient storage the in the air accumulator 15 by pneumatic filter 12 and gas pump 14;
H, its outlet nitrogen pot 16 in parallel with the outlet of this air accumulator 15 is arranged.Store in this nitrogen pot 16 for first and use and the sufficient nitrogen of usefulness as a supplement during periodic duty.Air accumulator 15 and nitrogen pot 16 exit in parallel has the pipeline of three parallel connections again again to the last period.Article one, pipeline is connected described thermophore heating tower's 6 bottom, carries the gaseous mixture that contains incondensable gas to participate in described burning carbon residue in thermophore heating tower 6, preheats the process (check valve that prevents that this part gaseous mixture from refluxing can be installed) of thermophore on this pipeline by this pipeline; Another pipeline is connected to the bottom of pyrolytic reaction tower 4, as the fluidized gas input pipe.On this fluidized gas input pipe, fluidized gas control valve 42 and Pressure gauge are installed.Article three, 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 15 with after mix in the exit of nitrogen pot 16 parallel connections, preheat the process of thermophore and enter the next working cycles except that a part is input into thermophore heating tower 6 confidential reference items, by the adjusting of fluidized gas control valve 42 and carrier gas control valve 21, back two ducted fluidized gas and carrier gas are 5.5～6.5 preceding the failing of relation continuation according to ratio.Wherein, enter next working cycles in the fluidized gas input pyrolytic reaction tower 4; 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 material in its pipe or further specializing of structure at wherein thermophore carbon residue circulation pipe 69 and thermophore loopback pipe 417.That is: in this routine apparatus system, thermophore carbon residue circulation pipe 69 tilts, and the arrival end of this circulation pipe 69 at initial separator 9 places is higher than the port of export of this circulation pipe 69 at thermophore heating tower 6 places; Equally, thermophore loopback pipe 417 also tilts, and the arrival end of this loopback pipe 417 at thermophore thermosistor 17 places is higher than the port of export of this loopback pipe 417 at pyrolytic reaction tower 4 places; The incline direction of two tipping tubes (69,417) and the angle of horizontal plane are all greater than 45 °.That is to say, in this example, be rely on thermophore and carbon residue (in the thermophore carbon residue circulation pipe 69) and preheated after the gravity of thermophore (in thermophore loopback pipe 417) self 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 carbon residue circulation pipe 69 and thermophore loopback pipe 417 and the angle of horizontal plane can also be bigger, and they can also be steeper in other words.
Embodiment 2:
This example is on the basis of summation part or embodiment 1, at the further optimization of pyrolytic reaction tower 4 heating rates, that is: a fluidized gas thermosistor 18 is set again on the pipeline that fluidized gas is input in the pyrolytic reaction tower 4.In other words, just in case the thermophore after preheating when also being not enough to improve heating rate in the pyrolytic reaction tower 4, just can carry out temperature adjustment to the fluidized gas of importing this pyrolytic reaction tower 4 with this fluidized gas thermosistor 18---preheating under the necessary situation.Simultaneously, also corresponding thermometer should be installed herein.Certainly, under the situation of conditions permit, this fluidized gas thermosistor 18 is good more the closer to the input port of pyrolytic reaction tower 4 bottoms.
Embodiment 3:
This example is on the basis of summation part, embodiment 1 or embodiment 2, at wherein with the circulation carrier gas living beings powder assist the further specific of mode of movement or structure.That is: in this routine apparatus system, described feed mechanism comprises helix transporting device 3 and is connected the outlet of this helix transporting device 3 and the feed pipe 19 between 4 imports of pyrolytic reaction tower, the version that inserts carrier gas input pipe in the feed mechanism and be with injector taps in its feed pipe 19, to allow the circulation carrier gas 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) with the mode of entrainmenting.Obviously, this example is that carrier gas dynamic pressure in the carrier gas input pipe is than the structure that is suitable under the higher condition of the pressure in the pyrolysis reaction tower 4.And, with this understanding, be more suitable in continuity production.
Embodiment 4:
If the carrier gas dynamic pressure in the carrier gas input pipe is unlike the pressure height in the pyrolytic reaction tower 4.Then on the basis of aforementioned structure, set up a branched pipe (with dashed lines draws in the accompanying drawing), the outlet of this branched pipe is tapped in the feeding device 2, on the charge door of this feeding device 2, install seal cover (drawing among the figure) additional at the waist of this carrier gas input pipe.Certainly, the structure that this paragragh is described still can be used for the carrier gas dynamic pressure than the high situation of pressure in the pyrolysis reaction tower 4, if just in order more to adapt to continuity production, when the condition of described pressure differential is set up, can stop up this branched pipe or close, open seal cover simultaneously and get final product.
In embodiment 3 and embodiment 4, can combine the rotational speed regulation (transporting velocity of decision helix transporting device 3) of the aperture of thermophore adjuster 51 being regulated with to adjustable frequency motor 1, according to different biomass materials and the thermal cracking situation in pyrolytic reaction tower 4 thereof, the mass ratio of thermophore of Tiao Jieing and living beings powder exactly.
If desired, in the apparatus system of embodiment 3 and embodiment 4, increase in all can feeding device 2 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 5:
This example is on the basis of embodiment 3 or embodiment 4, at the wherein further improvement of the structure of feed pipe 19.Its improved aspect is that feed pipe 19 is wrapped with cooling jacket 20.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 19, the situation of caking near the feed pipe 19 of pyrolytic reaction tower 4 import departments even owing to pyrolytic reaction tower 4.
From the invention scheme and the specific embodiment be not difficult to find out that except that the small part thermal lift, the circulation power of native system mainly comes from gas pump 14.Obviously, the supply gas pressure of this gas pump 14 and flow can be regulated.
Following table is the part test data (powder particle diameter＜1mm in the table of embodiment 5.Other parameter areas that the living beings of other raw materials of 1mm＜powder particle diameter＜2mm and the present invention are disclosed are by other experiment confirms.After those skilled in the art has understood the present invention, equally also can normally analyze, inference comes out):
| |
1 | 2 | 3 | 4 | 5 | ||
| Biomass material | The eucalyptus sawdust | The pine branch powder | The rice straw powder | The bean dregs powder | The wheat straw powder | ||
| Preliminary treatment | Moisture content | 7.8％ | 6.5％ | 7.0％ | 6.3％ | 7.5％ | |
| Powder particle size range (mm) (sieve number) | 0.61～0.95 (20～30) | 0.30～0.44 (40～60) | 0.44～0.61 (30～40) | 0.36～0.44 (40～50) | 0.30～0.44 (40～60) | ||
| The flow ratio of circular flow gasification and circulation carrier gas (error ± 5%) | 5.5 | 6.4 | 6.2 | 5.8 | 5.9 | ||
| The addition of living beings powder (kg/h) | 5.5±0.1 | 15±0.3 | 12±0.3 | 8±0.2 | 15±0.3 | ||
| The quality ratio of thermophore and living beings powder (error ± 5%) | 3.5 | 4.5 | 2.2 | 3.8 | 4.5 | ||
| By heating rate in the pre-heating temperature of fluidized gas and thermophore and the determined pyrolytic reaction tower of flow thereof (℃/s) | 820±30 | 950±30 | 580±30 | 900±30 | 870±30 | ||
| In the pyrolytic reaction tower | Pressure (Mpa) | 0.09～0.11 | 0.08～0.11 | 0.10～0.12 | 0.10～0.12 | 0.09～0.11 | |
| Temperature (℃) | 420±20 | 480±20 | 450±20 | 510±20 | 550±20 | ||
| The cooldown rate of pyrolysis gas in condenser (℃/s) | 620±20 | 500±20 | 450±25 | 750±30 | 680±20 | ||
| Liquefied fraction (mass ratio) | 53.6％ | 58.4％ | 38.5％ | 43.6％ | 41.7％ | ||
Claims (8)
1, the process of biomass pyrolysis liquefaction, it comprises by feed mechanism sends into biological material the interior step of pyrolytic reaction tower (4), 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 (4), in separator, pyrolysis gas and solid matter are carried out the step of gas solid separation, and in condenser (11) 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 (4) is 0.08～0.12MPa, and temperature range is 400～570 ℃, and the heating rate of living beings powder in pyrolytic reaction tower (4) is 500～1000 ℃/s; The living beings powder is sent in the interior step of pyrolytic reaction tower (4) 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 (4) after, its thermophore is sent in pyrolytic reaction tower (4) with pyrolysis gas, carbon residue and ash; Then, there is one thermophore and carbon residue and pyrolysis gas and ash separation steps;
D, in the step of described gas solid separation, be that pyrolysis gas separates with ash; When entering the gas solid separation step, thermophore of separating suddenly in previous step and carbon residue enters a burning carbon residue, to preheat the step of thermophore;
E, preheat thermophore after, enter a step that this thermophore and waste gas and ash are separated;
F, the thermophore of separating enter one it are carried out the step of temperature adjustment; Then, there is one the thermophore after the temperature adjustment sent in the pyrolytic reaction tower (4) for the step that recycles again; Entering the interior thermophore of pyrolytic reaction tower (4) and the quality ratio of living beings powder is 1.8～4.6; Simultaneously, there is the heat of waste gas that a utilization separates and ash to preheat the step of combustion air; Combustion air after preheated is admitted to the described burning carbon residue of steps d, preheat carry out in the step of thermophore combustion-supporting;
G, after the gas solid separation described in the d step is finished, isolated pyrolysis gas enters the step that is condensed into bio oil; In condenser (11), 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 (11) with after the bio oil of condensation is separated, collect as reclaiming gas;
H, recovery gas mix with the nitrogen that replenishes; Defeated before mixed gas divides three the tunnel to continue, one road band that contained incondensable gas enters described burning carbon residue in this recovery gas, preheat in the step of thermophore and burn with carbon residue; Two-way is pressed flow ratio 5.5～6.5 distribution more in addition; 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; A road of large percentage is input in the pyrolytic reaction tower (4) once more as fluidized gas.
2, realize the double tower apparatus system of the process of the described biomass pyrolysis liquefaction of claim 1, it is characterized in that this apparatus system comprises: the interior carrier gas input pipe of feeding device (2), feed mechanism and access feed mechanism that performing step b is used; The living beings powder is carried out the pyrolytic reaction tower (4) of thermal cracking, and this pyrolytic reaction tower (4) is vertically placed, and the bottom is provided with wind distributing hole plate (41); The initial separator (9) that thermophore and carbon residue and pyrolysis gas and ash are separated; Burn within it carbon residue, with the thermophore heating tower (6) that preheats thermophore and this thermophore heating tower of UNICOM (6) thereof thermophore carbon residue circulation pipe (69) with initial separator (9); The thermophore separator (5) that thermophore after this heating and waste gas and ash are separated; The thermophore of separating is carried out the thermophore thermosistor (17) of temperature adjustment and the thermophore after the temperature adjustment is imported the into interior thermophore loopback pipe (417) of pyrolytic reaction tower (4); Allow heat exchanger that the high-temp waste gas separated and ash preheat combustion air and the air blast of carrying combustion air; The gas-solid separator (10) that pyrolysis gas and ash are separated; Condensation goes out the condenser (11) and the oil catcher (13) thereof of bio oil from pyrolysis gas, collects the air accumulator (15) and the gas pump (14) thereof that reclaim gas; The nitrogen pot (16) that its outlet is in parallel with the outlet of air accumulator (15); And the pipeline of connection said apparatus and corresponding control valve, Pressure gauge and the thermometer on pipeline.
3, the double tower apparatus system of the process of realization biomass pyrolysis liquefaction according to claim 2, it is characterized in that, described thermophore carbon residue circulation pipe (69) tilts, and the arrival end that this circulation pipe (69) is located in initial separator (9) is higher than the port of export that this circulation pipe (69) is located thermophore heating tower (6); Described thermophore loopback pipe (417) tilts, and the arrival end that this loopback pipe (417) is located at thermophore thermosistor (17) is higher than the port of export that this loopback pipe (417) is located at pyrolytic reaction tower (4); The incline direction of two tipping tubes (69,417) and the angle of horizontal plane are all greater than 45 °.
According to the double tower apparatus system of the process of claim 2 or 3 described realization biomass pyrolysis liquefactions, it is characterized in that 4, fluidized gas is input on the pipeline in the pyrolytic reaction tower (4) a fluidized gas thermosistor (18).
5, according to the double tower apparatus system of the process of claim 2 or 3 described realization biomass pyrolysis liquefactions, it is characterized in that, described feed mechanism comprises the feed pipe (19) of helix transporting device (3) and outlet that is connected this helix transporting device (3) and pyrolytic reaction tower (4) import, and the version that inserts carrier gas input pipe in the feed mechanism and be with injector taps in its feed pipe (19).
6, the double tower apparatus system of the process of realization biomass pyrolysis liquefaction according to claim 4, it is characterized in that, described feed mechanism comprises the feed pipe (19) of helix transporting device (3) and outlet that is connected this helix transporting device (3) and pyrolytic reaction tower (4) import, and the version that inserts carrier gas input pipe in the feed mechanism and be with injector taps in its feed pipe (19).
7, the double tower apparatus system of the process of realization biomass pyrolysis liquefaction according to claim 5 is characterized in that, is wrapped with cooling jacket (20) at described feed pipe (19).
8, the double tower apparatus system of the process of realization biomass pyrolysis liquefaction according to claim 6 is characterized in that, is wrapped with cooling jacket (20) at described feed pipe (19).
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