CN105199759A - Biomass liquefaction thermal cracking system - Google Patents
Biomass liquefaction thermal cracking system Download PDFInfo
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- CN105199759A CN105199759A CN201410302164.XA CN201410302164A CN105199759A CN 105199759 A CN105199759 A CN 105199759A CN 201410302164 A CN201410302164 A CN 201410302164A CN 105199759 A CN105199759 A CN 105199759A
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- distributor
- scission reaction
- reaction pipe
- splitting system
- thermal
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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Abstract
The invention relates to a biomass liquefaction thermal cracking system. The feeding device part of the system uses the flue gas generated during the reaction in a cracking unit to preheat raw materials, and meanwhile pushes the raw materials to a feeding station; after being subjected to drying, air filtering and flue gas filtering, the raw materials enter a material distributing device; a uniform feeding device is mounted in the material distributing device; the uniform feeding device can be a plate grid; an oscillator can be mounted according to needs, so as to realize that the materials can uniformly enter a cracking reaction tube for cracking under the anaerobic and dry state.
Description
Technical field
The present invention relates to the technical field utilizing biomass material to obtain the energy, particularly relate to a kind of biomass liquefying thermal splitting system.
Background technology
Being that raw material carries out regeneration and produces combustible fuel with biomass, is the key areas of energy recycling.Test multiple technologies equipment both at home and abroad, to reach the object increasing bio oil productive rate and improve energy utilization.In prior art scission reaction process, some equipment needs to carry out feeding and anoxybiotic process with nitrogen as carrier gas picks material, but nitrogen use level is very large, need thermal pretreatment, so running cost is high, and the raw material be fed in prior art in scission reaction pipe is uneven, heats also uneven in thermal cracking processes, so just affect heat transfer efficiency, and then affect preparation of fuel efficiency.
In order to solve existing heat of liquefaction cracker Problems existing, the present inventor is substantially in being engaged in this type of product design application practical experience for many years and expertise, actively in addition research and innovation, after constantly studying and improving, creates the present invention had practical value finally.
Summary of the invention
Main purpose of the present invention is, overcome in biomass pyrolysis for liquid production technique and there is the not high problem of energy utilization rate, carry out the heat recovery and utilization of high-temperature flue gas, effectively utilize the waste heat of flue gas, thus realize autothermal, free of contamination biomass liquefying thermal cracking process, improve efficiency of energy utilization, cost-saving
Another object of the present invention is to, overcome feeding problem of non-uniform, solve this technical problem and distributor is set above scission reaction pipe, thus the heating of solution Raw is uneven, affects lysis efficiency.
Another object of the present invention is to, overcome thermo-cracking efficiency in scission reaction pipe, reconcile the pipe diameter of scission reaction pipe according to the density of inlet amount and material, Ceramic Balls can also be installed additional in pipeline.
The object of the invention to solve the technical problems realizes by the following technical solutions, according to the biomass liquefying thermal splitting system that the present invention proposes, comprise device for feeding raw materials, thermal cracker, fuel treating equipment, wherein scission reaction pipe arranges distributor and heat scission reaction pipe above comprising, and distributor is built with even pay-off.Have one-level, secondary heat exchanger at the install pipeline in high-temperature flue gas exit, scission reaction pipe upper end, the air entered is preheating material under interchanger effect.
The object of the invention to solve the technical problems can also by realizing with technical measures further, and in wherein said distributor, evenly pay-off can be cross grid, and the grid number of plies adjusts according to material quantity.
The object of the invention to solve the technical problems by realizing further with technical measures, in order to realize even feeding further, can also improve feeding speed simultaneously, can arrange vibratile grid in distributor.
The object of the invention to solve the technical problems can also be realized further by following technical measures, furnace tubing in scission reaction pipe, according to inlet amount adjusting pipe diameter, can install Ceramic Balls additional time material density is little or time inlet amount is large in pipe.
Can know via above-mentioned, biomass liquefying thermal splitting system pay-off part of the present invention utilizes strong solution device to react the smoke pre-heating raw material produced, promote raw material to feeding station simultaneously, distributor is entered after super-dry, filter sky, the process of filter cigarette, even pay-off is installed in distributor, even pay-off can be grid, installs vibrator additional as required, realizes material and under anoxybiotic, drying regime, evenly enters scission reaction pipe carry out cracking.
By technique scheme, the present invention at least has following advantages:
(1) greatly reduce heat energy consumption, achieve no pollution discharge.The thermal splitting system that the present invention proposes achieves autothermal, free of contamination biomass liquefying thermal cracking process, improves efficiency of energy utilization, cost-saving, thus solves that the heating raw materials existed in prior art is uneven, the not high defect of lysis efficiency.
(2) compared to the prior art, the thermal splitting system that the present invention proposes substantially increases feed processing capacity, manageable material is extensive, both can be wood chip, also can be agricultural crop straw, granularity is within 1 centimetre, and prior art only can process the material that granularity is less than 0.5 millimeter.
(3) compared to the prior art, the pyrolysis reaction device charging of the thermal splitting system that the present invention proposes is even, and lysis efficiency is high, greatly reduces the coking of heat scission reaction pipe, thus the maintenance cycle of existing installation 5-6 days is extended to about 1 month.
(4) the present invention is by the setting of distributor, and by the mixing of stack gas and material, ensure that in charging there is no air (anaerobism), solve prior art and use the defect that nitrogen convey materials cost is high, solve the technological deficiency that prior art feeding is uneven simultaneously.
(5) inlet amount of thermal splitting system provided by the invention according to material and the kind of raw material, charging caliber and the quantity of material in scission reaction pipe can be adjusted, Ceramic Balls can also be installed additional, better be beneficial to the scission reaction efficiency of material, thus achieve three integration of function of vacuum bed, moving-bed and fluidized-bed.
Above-mentioned explanation is only the general introduction of technical solution of the present invention, in order to better understand technique means of the present invention, and can be implemented according to the content of specification sheets, coordinates accompanying drawing to describe in detail below with present pre-ferred embodiments.
Accompanying drawing explanation
Fig. 1 is biomass liquefying thermal splitting system structural representation of the present invention.
Fig. 2 is distributor and interior grid schematic diagram thereof in biomass liquefying thermal splitting system of the present invention.
In figure, 1-ingredient conveyor; 2-raw material storage batch turning station; 3-rotary valve; 4-Venturi tube; 5-one-level hopper; 6-filters empty drying installation; 7-rotary valve; 8-Venturi; 9-secondary hopper; 10-filters cigarette drying installation; 11-rotary valve; 12-distributor; 13-scission reaction pipe; 14-powdered carbon subsider; 15-first-class heat exchanger; 16-secondary heat exchanger; 17-combustion air blower fan; 18-one-level carries material blower fan; 19-secondary carries material blower fan.I-raw material; II-air; III-warm air; IV-natural gas; V-powdered carbon subsequent disposal; The process of VI-washing tower; VII-flue gas is emptying; VIII-air is emptying.
Embodiment
In order to further set forth the present invention for the technique means reaching predetermined goal of the invention and take and effect, below in conjunction with accompanying drawing and preferred embodiment, to its embodiment of biomass liquefying heat scission reaction system proposed according to the present invention, step, structure, feature and effect thereof, describe in detail.
Refer to shown in Fig. 1, the implementing procedure of biomass liquefying heat scission reaction system of the present invention is as follows:
Biomass material is crushed to below 1cm, and raw material batch turning storehouse 2 delivered to by transfer roller 1, opens changeover valve 3, and raw material enters Venturi 4, and under the preheating and pushing effect of warm air, deliver to one-level hopper 5, feeding amount is controlled by changeover valve 3; Raw material is after the empty drying installation 6 of filter that one-level hopper 5 upper end connects carries out anaerobic drying treatment, open rotary valve 7, raw material enters secondary hopper 9 under being promoted by the high-temperature flue gas that Venturi 8 enters, the filter cigarette drying installation 10 connected through secondary hopper upper end carries out redrying deoxygenation process, and then treated raw material delivers to scission reaction pipe by distributor 12; One-level hopper, secondary hopper and distributor top are closed, changeover valve 3,7, open during 11 difference, guarantee that the raw material in distributor carries in anaerobic drying regime.
Material is in scission reaction pipe after high temperature rapid cleavage, and the high-temperature flue gas that upper outlet flows out becomes air II heating into warm air III through first-class heat exchanger 15, and warm air is in scission reaction pipe lower end inlet mouth and the mixed firing of natural gas inlet mouth.
The air II that above-mentioned high-temperature flue gas enters outside secondary heat exchanger 16 preheating, air through preheating enters Venturi 4, heating and promotion raw material enter one-level hopper, enter Venturi 8 through changing the civilian flue gas of heat treated height, and preheating, promotion raw material enter secondary hopper.
Above one-level hopper, be connected with the empty drying process device 6 of filter, this device connects emptying pipe.
Above secondary hopper, be connected with filter cigarette drying process device 10, this device connects smoke discharging pipe.
The top of scission reaction pipe is provided with distributor, and distributor is rounding bench-type, and the inside is provided with grid, and grid is right-angled intersection arrangement, and material is uniform under the effect of stack gas sends into cracking pipeline.
In order to better realize even quick feeding, on distributor, vibrator can be installed.
Pyrolyzer top adopts flat kiln with movable roof top form, and divide four layers in pyrolyzer, amount to 12 high speed dual fuel burners 12,32 high-temperature resistant radiation pipes, maximum operation (service) temperature reaches 1100 DEG C.
Through the product that cracking obtains, enter powdered carbon subsider 14 and process, in subsider internal upper part port, feed pipe is installed, as shown in Fig. 2 sedimentation grain sectional view, wherein outside powdered carbon sedimentation grain top gas-solid feed-pipe, disc punches, communicate with bore; Gas-solid mixture enters in the pipeline on powdered carbon subsider top, and gas is disengaged by the pore of pipeline, then carries out carrying out washing treatment VI, and solid matter enters subsequent disposal V in powdered carbon subsider bottom.
Natural gas IV input aperture and warm air III input aperture igniting generation flue gas first by scission reaction pipe lower end when equipment runs, then flue gas is by first-class heat exchanger warm-up combustion-supporting air, by secondary heat exchanger preheating material, and then raw material sent into by the rotary valve opened below distributor.
It is open when changeover valve 3,7,11 is different.
Raw material can be wood chip, agricultural crop straw, and granularity is not more than 1cm.
Native system working process also comprises following Controlling System.
Combustion control system: ratio burns the fuzzy control is all carried out in combustion air and the combustion gas of full kiln, according to the requirement heated up, the size of combustion air and combustion gas aperture by degree according to the curve of setting in proportion from line trace, control accuracy can reach ± and 3 DEG C, in kiln, the burner of staggered arrangement can make the temperature difference in kiln control at ± 10 DEG C in the whole temperature rise period up and down.
Warning: each blower fan has failure warning system; The setting of kiln temperature upper and lower limit is reported to the police, and the setting of pressure upper and lower limit is reported to the police; Each opening of device fault alarm.Burner is equipped with automatic ignitor and flame detector, and flame-out cut-out automatically, operational safety is reliable.
Temperature controlling system: temperature control principle is: thermopair detecting temperature-temperature controller (design temperature)-performer-combustion air volume-ratio adjusting valve-gas flow, thus control firing temperature.The main method of this Systematical control is: detect kiln temperature numerical value by thermopair, temperature controller is sent to by compensating lead wire, compare produced difference to be outputed signal by PID arithmetic feed back to performer with set(ting)value, combustion air volume is regulated by the positive and negative rotation of performer, control kiln temperature by combustion air volume passing ratio variable valve adjustment of combustion gas flow, change kiln atmosphere as required.
Equipment interlocking: gas safe runs when starting and first opens smoke exhaust fan, and time-delay closing diffuses magnetic valve and automatically opens fuel manifold magnetic valve, then opened smoke-discharging blower fan.Run chain, after burner blower stops, automatically close fuel main valve, open diffusion valve.Instrument is the intelligent instrument of PID function, realizes chain and management.All instrument, low-voltage electrical and portions of electronics components and parts etc. are mainly import, joint or domestic performance comparatively stable product, are convenient to maintenance and replace.
In one embodiment, divide 4 layers in scission reaction pipe, be inside provided with 12 dual fuel burners, the burner of fuel burner is in interior upper and lower staggered arrangement.Scission reaction pipe is high temperature material radiator tube, and adds Ceramic Balls as thermal barrier.
In one embodiment, the quantity of scission reaction pipe is 4.
Consult further shown in Fig. 1, invention further provides a kind of method that biomass through pyrolysis produces biofuel, it comprises the following steps:
Biomass material is crushed to below 1cm, and raw material batch turning storehouse 2 delivered to by transfer roller, and open changeover valve 3 raw material and deliver to one-level hopper 5 under the preheating and pushing effect of warm air, feeding amount is controlled by changeover valve; Raw material is after the air filter 8 that one-level hopper upper end connects carries out anaerobic drying treatment, secondary hopper 9 is mixed into by discharge valve and flue gas, enter distributor 12 after the smoke abatement drying installation 10 connected through secondary hopper 9 upper end processes, open changeover valve 11 and biological raw material is delivered to scission reaction pipe; One-level hopper 5, secondary hopper 9 and distributor 12 top are closed, open when changeover valve 3,6,11 is different, guarantee that the raw material in distributor is in anaerobic drying regime;
Carry out after scission reaction terminates when biomass material is in scission reaction pipe 13, its gas-solid mixture produced is sent to powdered carbon sedimentation grain;
The flue gas that scission reaction pipe upper outlet 16 produces is through one-level exchanging air heating combustion air;
The flue gas that scission reaction pipe upper outlet (16) produces is heated through secondary heat exchange gas by Venturi tube 4 and is promoted raw material and enters one-level hopper;
The flue gas that scission reaction pipe upper outlet 16 produces is discharged through an air cooler part, and a part is heated by Venturi tube 7 and promoted raw material and enters secondary hopper;
Gas-solid mixture enters the pipeline on powdered carbon subsider top, and gas is disengaged by the pore on pipe surface, and the outlet through powdered carbon subsider top enters rinse bath, after washing, obtain biofuel;
Solid matter enters refrigerating unit cooling at powdered carbon subsider.
In one embodiment, first pass through the combustion gas input aperture in scission reaction pipe lower end and combustion air blower fan input aperture igniting generation flue gas, then flue gas is by first-class heat exchanger warm-up combustion-supporting air, by secondary heat exchanger preheating material, and then raw material sent into by the rotary valve opened below distributor.
In one embodiment, first open smoke exhaust fan when gas safe runs, time-delay closing diffuses thermoelectrical magnetic valve and automatically opens fuel manifold magnetic valve, then opened smoke-discharging blower fan, runs chain, and burner blower stops, and automatically closes fuel main valve, opens diffusion valve.
In one embodiment, ratio burns the fuzzy control is all carried out in the combustion air of full kiln and combustion gas, according to the requirement heated up, the size of combustion air and combustion gas aperture by degree according to the curve of setting in proportion from line trace, control accuracy can reach ± and 3 DEG C, in kiln, the burner of staggered arrangement can make the temperature difference in kiln control at ± 10 DEG C in the whole temperature rise period up and down
In one embodiment, each blower fan is all connected with pressure control device.
In one embodiment, kiln temperature is set with temperature alarm system up and down, pressure alarm system.
Refer to shown in Fig. 2, its display be the schematic diagram of distributor in one embodiment of the invention, comprise the schematic diagram that inside can vibrate grid.Wherein, distributor 2a is outside schematic diagram, does not show the internal structure of distributor.Distributor is rounding bench-type, and the diameter of the one end be connected with scission reaction pipe 13 is suitable with the diameter of scission reaction pipe, but little compared with the diameter of its other end.2b display in figure be the grid structure schematic diagram longitudinally arranged in distributor, the 2c display in figure be the grid structure schematic diagram of lateral arrangement in distributor, 2b and 2c intersects and prevents.Wherein grid can be angled being obliquely installed, and is preferably 20 °, as shown in 2d.The grid that arranges of certain angle is conducive to the sieving of raw material and even feeding.Raw material after sieving enters scission reaction pipe 13 according to the direction of 2e.
The above, it is only preferred embodiment of the present invention, not any pro forma restriction is done to the present invention, although the present invention discloses as above with preferred embodiment, but and be not used to limit the present invention, any those skilled in the art, do not departing within the scope of technical solution of the present invention, when the method and technology contents that can utilize above-mentioned announcement are made a little change or be modified to the Equivalent embodiments of equivalent variations, in every case be the content not departing from technical solution of the present invention, according to any simple modification that technical spirit of the present invention is done above embodiment, equivalent variations and modification, all still belong in the scope of technical solution of the present invention.
Claims (6)
1. a biomass liquefying thermal splitting system, comprises device for feeding raw materials, thermal cracker, biomass fuel material processing device, it is characterized in that, wherein said thermal cracker comprises scission reaction pipe and distributor, and described distributor one end is directly connected with one end of described scission reaction pipe.
2. biomass liquefying thermal splitting system according to claim 1, it is characterized in that, described distributor is rounding bench-type shape, the diameter of one end that described distributor is directly connected with described scission reaction pipe is suitable with the diameter of described scission reaction pipe, and is less than the diameter of the described distributor the other end.
3. biomass liquefying thermal splitting system according to claim 1 and 2, is characterized in that being provided with even pay-off in described distributor, and described even pay-off is made up of one or more layers right-angled intersection grid vibratile.
4. biomass liquefying thermal splitting system according to claim 1 and 2, it is characterized in that being equiped with carrier in described scission reaction pipe, described carrier is selected from Ceramic Balls or quartz sand.
5. biomass liquefying thermal splitting system according to claim 1, it is characterized in that described device for feeding raw materials comprises raw material storage batch turning station, rotary valve (3) connects Venturi (4), Venturi (4) one end connects secondary heat exchanger outlet, the other end connects one-level hopper (5), one-level hopper upper end connects raw material and filters empty device (8), lower end connects secondary hopper (9) by rotary valve (6) and Venturi (7), secondary hopper upper end connects smoke evacuation drying installation (10), lower end connects distributor (12) by rotary valve (11).
6. biomass liquefying thermal splitting system according to claim 1, wherein said fuel treating equipment comprises powdered carbon subsider, wherein outside powdered carbon sedimentation grain top gas-solid feed-pipe, disc punches, communicates with bore.
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| CN201410302164.XA CN105199759A (en) | 2014-06-27 | 2014-06-27 | Biomass liquefaction thermal cracking system |
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| CN201410302164.XA CN105199759A (en) | 2014-06-27 | 2014-06-27 | Biomass liquefaction thermal cracking system |
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Citations (6)
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|---|---|---|---|---|
| RU2277115C1 (en) * | 2004-11-09 | 2006-05-27 | Государственное унитарное предприятие "Институт нефтехимпереработки" Республики Башкортостан (ГУП "ИНХП"РБ) | Reactor for the liquid-phase thermal cracking |
| CN1962818A (en) * | 2005-11-08 | 2007-05-16 | *** | Process for preparing bio-oil by using rapid thermal cleavage technology |
| CN101280199A (en) * | 2008-05-14 | 2008-10-08 | 合肥工业大学 | High-temperature low-tar biomass gasifier |
| CN101899315A (en) * | 2010-07-14 | 2010-12-01 | 青岛大学 | Device for preparing bio-oil from biomass through pyrolysis |
| CN102757802A (en) * | 2012-07-23 | 2012-10-31 | 李柯 | Gas-heat-carrier full-circulation square furnace |
| CN102206496B (en) * | 2011-04-19 | 2013-06-19 | 山东理工大学 | Pyrolysis and liquidation system for heating biomass by using solid heat storage ball |
-
2014
- 2014-06-27 CN CN201410302164.XA patent/CN105199759A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2277115C1 (en) * | 2004-11-09 | 2006-05-27 | Государственное унитарное предприятие "Институт нефтехимпереработки" Республики Башкортостан (ГУП "ИНХП"РБ) | Reactor for the liquid-phase thermal cracking |
| CN1962818A (en) * | 2005-11-08 | 2007-05-16 | *** | Process for preparing bio-oil by using rapid thermal cleavage technology |
| CN101280199A (en) * | 2008-05-14 | 2008-10-08 | 合肥工业大学 | High-temperature low-tar biomass gasifier |
| CN101899315A (en) * | 2010-07-14 | 2010-12-01 | 青岛大学 | Device for preparing bio-oil from biomass through pyrolysis |
| CN102206496B (en) * | 2011-04-19 | 2013-06-19 | 山东理工大学 | Pyrolysis and liquidation system for heating biomass by using solid heat storage ball |
| CN102757802A (en) * | 2012-07-23 | 2012-10-31 | 李柯 | Gas-heat-carrier full-circulation square furnace |
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