CA2821474C - Compact fast pyrolysis system for conversion of carbonacous materials to liquid, solid and gas - Google Patents
Compact fast pyrolysis system for conversion of carbonacous materials to liquid, solid and gas Download PDFInfo
- Publication number
- CA2821474C CA2821474C CA2821474A CA2821474A CA2821474C CA 2821474 C CA2821474 C CA 2821474C CA 2821474 A CA2821474 A CA 2821474A CA 2821474 A CA2821474 A CA 2821474A CA 2821474 C CA2821474 C CA 2821474C
- Authority
- CA
- Canada
- Prior art keywords
- biomass
- auger
- inlet
- outlet
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B7/00—Coke ovens with mechanical conveying means for the raw material inside the oven
- C10B7/10—Coke ovens with mechanical conveying means for the raw material inside the oven with conveyor-screws
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
- C10B49/20—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Dispersion Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The present invention relates to an apparatus for pyrolysis of organic material biomass, comprising: i) a first, horizontal auger tube having inlet for a heat carrier and a second inlet for biomass; and a first outlet for pyrolysis gas and a second outlet for said heat carrier and transformed biomass; ii) a second, inclined auger tube having an inlet at or below the second outlet of said first auger tube, to receive the heat carrier and transformed biomass from the second outlet of the first auger tube and an outlet at a level above the inlet thereof, said outlet communicating with the first inlet of the first auger tube to deliver heat carrier thereto.
Description
Compact Fast Pyrolysis System for Conversion of Carbonacous Materials to Liquid, Solid and Gas The present invention relates to the field of biomass pyrolysis, and provides a compact, substantially self contained fast pyrolysis system and apparatus for conversion of biomass into solid, liquid and gas pyrolysis products.
BACKGROUND OF THE INVENTION
Biomass pyrolysis in itself is not a new technology and the literature abounds with examples of various types of pyrolysis units. It is generally accepted that biomass pyrolysis can be carried out in either a fast mode or a slow mode. The fast mode maximizes liquid yield, while the slow mode maximizes solid (charcoal) yield. Lede (2013) published an extensive review and description of fast pyrolysis systems. The extensive reference list is testimony to the volume of literature available on pyrolysis. The following is a list of fast pyrolysis processes including but not restricted to circulating bed (Fred l ), fluid bed (Piskorz et al,) twin auger ( Brown, 2009 or single auger (Hornung, Fransham). Virtually all fast pyrolysis systems involve mixing the biomass with a heat carrier. Silica sand is the most often used, although steel shot (Fransham), steel balls (Hornung) or ceramic shot is used in most auger pyrolysis. When the heat carrier is circulated with recycled gas, sand is the heat carrier of choice. The general object of fast pyrolysis is to drive off volatiles from biomass material and condense them in a
BACKGROUND OF THE INVENTION
Biomass pyrolysis in itself is not a new technology and the literature abounds with examples of various types of pyrolysis units. It is generally accepted that biomass pyrolysis can be carried out in either a fast mode or a slow mode. The fast mode maximizes liquid yield, while the slow mode maximizes solid (charcoal) yield. Lede (2013) published an extensive review and description of fast pyrolysis systems. The extensive reference list is testimony to the volume of literature available on pyrolysis. The following is a list of fast pyrolysis processes including but not restricted to circulating bed (Fred l ), fluid bed (Piskorz et al,) twin auger ( Brown, 2009 or single auger (Hornung, Fransham). Virtually all fast pyrolysis systems involve mixing the biomass with a heat carrier. Silica sand is the most often used, although steel shot (Fransham), steel balls (Hornung) or ceramic shot is used in most auger pyrolysis. When the heat carrier is circulated with recycled gas, sand is the heat carrier of choice. The general object of fast pyrolysis is to drive off volatiles from biomass material and condense them in a
2 matter of seconds. Slow pyrolysis processes include augers (Flottvik), multiple hearth and batch systems used in the coking industry. Slow pyrolysis systems do not generally use a heat carrier and is generally carried out in a matter of minutes. People skilled in the art will recognize that other possible processes also exist for conducting pyrolysis.
Circulating bed type fast pyrolysis systems (Freel) also known as transport bed processes involve moving sand vertically in a tube at velocities in the order of 20 m/sec. The motivating gas is oxygen free recycled gas obtained after all of the condensable volatiles have been stripped from the non¨condensing gas. Biomass enters the vertical tube at a point above the base of the tube. The biomass mixes with the sand in the tube and the volatile matter in the biomass is converted to a hot gas. There are however, fundamental problems with transport beds. The first is the use of sand as a heat carrier. Sand has a low thermal conductivity and the sand temperature has to be high enough to transfer sufficient energy to raise the biomass temperature to approximately 515 C. However, the short contact time and the low thermal conductivity of sand mean that only a fraction of the energy contained in the sand grain can be transferred to the biomass. Also, the large amount of recycled gas that is required for transport is a parasitic load on the system. The gas has to be heated and cooled for each cycle. Condensers have to be large enough to handle the heat load in the gas stream. The excessive electrical energy required to transport sand several meters vertically in the air at velocities of about 20 m/sec. greatly reduces the efficiency of the process.
Furthermore the sand and biomass are in a dispersed low density mixture of sand, biomass
Circulating bed type fast pyrolysis systems (Freel) also known as transport bed processes involve moving sand vertically in a tube at velocities in the order of 20 m/sec. The motivating gas is oxygen free recycled gas obtained after all of the condensable volatiles have been stripped from the non¨condensing gas. Biomass enters the vertical tube at a point above the base of the tube. The biomass mixes with the sand in the tube and the volatile matter in the biomass is converted to a hot gas. There are however, fundamental problems with transport beds. The first is the use of sand as a heat carrier. Sand has a low thermal conductivity and the sand temperature has to be high enough to transfer sufficient energy to raise the biomass temperature to approximately 515 C. However, the short contact time and the low thermal conductivity of sand mean that only a fraction of the energy contained in the sand grain can be transferred to the biomass. Also, the large amount of recycled gas that is required for transport is a parasitic load on the system. The gas has to be heated and cooled for each cycle. Condensers have to be large enough to handle the heat load in the gas stream. The excessive electrical energy required to transport sand several meters vertically in the air at velocities of about 20 m/sec. greatly reduces the efficiency of the process.
Furthermore the sand and biomass are in a dispersed low density mixture of sand, biomass
3 and motivating gas. Heat transfer from the sand to the biomass is predicated on the random contact between the sand grains and the biomass particles.
Fluid bed pyrolysis processes have similar short comings to circulating bed reactors. Fluid beds have to be shallow to ensure short vapour residence times required to limit secondary chemical reactions. Preventing carryover of the sand into the char recovery circuit requires balancing of sand size and airflow. A further limitation is the transferring of heat into the bed.
The only ability to do pyrolysis work is dictated by the mass of gas multiplied by the temperature differential between the incoming and exiting recycle gas multiplied by the specific heat of the recycle gas. Large blowers are required to move the recycled fluidizing gas. The key technical challenge is to scale up the reactor to meet the demands of short residence time while maintaining the sand in the reactor. The sand in the fluid bed is in a low density medium and contact between the sand particle and the incoming biomass relies on rapid mixing before a large bubble of gas rises to the bed surface and expands outwardly.
There is therefore a considerable technical challenge to feeding biomass into large reactors and separating reacted biomass (charcoal) from sand. Attempts have been made to scale up fluid bed reactors for pyrolysis. No biofuel pyrolysis plant is currently operating at a commercial scale using this technology.
Auger pyrolysis offers a solution to the deficiencies in the fluid bed and circulating bed processes. Steel shot has a higher thermal conductivity than sand and hence more energy can be transferred at a lower operating temperature from the shot to the biomass in an equivalent
Fluid bed pyrolysis processes have similar short comings to circulating bed reactors. Fluid beds have to be shallow to ensure short vapour residence times required to limit secondary chemical reactions. Preventing carryover of the sand into the char recovery circuit requires balancing of sand size and airflow. A further limitation is the transferring of heat into the bed.
The only ability to do pyrolysis work is dictated by the mass of gas multiplied by the temperature differential between the incoming and exiting recycle gas multiplied by the specific heat of the recycle gas. Large blowers are required to move the recycled fluidizing gas. The key technical challenge is to scale up the reactor to meet the demands of short residence time while maintaining the sand in the reactor. The sand in the fluid bed is in a low density medium and contact between the sand particle and the incoming biomass relies on rapid mixing before a large bubble of gas rises to the bed surface and expands outwardly.
There is therefore a considerable technical challenge to feeding biomass into large reactors and separating reacted biomass (charcoal) from sand. Attempts have been made to scale up fluid bed reactors for pyrolysis. No biofuel pyrolysis plant is currently operating at a commercial scale using this technology.
Auger pyrolysis offers a solution to the deficiencies in the fluid bed and circulating bed processes. Steel shot has a higher thermal conductivity than sand and hence more energy can be transferred at a lower operating temperature from the shot to the biomass in an equivalent
4 period of time as compared to sand reactors. Fransham (2001) developed an auger system whereby the shot was recirculated via a bucket elevator. The charcoal and non¨condensing gases were burned to provide process heat. The system relied on pressure from the expanding raw pyrolysis gas and the volume reduction in the gas at the first stage condensing unit to move the gas from the reactor to the condensers with a residence time similar to that of the other pyrolysis systems. The advantage of the auger system is the biomass is in close contact with the heat carrier and hence high heating rates are achieved. The use of steel shot over sand significantly reduces auger wear and heat carrier attrition when compared to sand filled reactors.
Hornung used hollow steel balls to rapidly pyrolyze biomass and separated the charcoal from the balls in a trommel screen. The balls were heated and circulated in a system of screw conveyors. This system has been used for a variety of applications and numerous papers have been written and patents filed on results from this process.
SUMMARY OF THE INVENTION
Auger pyrolysis has been shown above to be an improvement on the fluid bed and circulating bed pyrolysis systems. This invention is an improvement and simplification of the auger pyrolysis system developed by Fransham (2001). There are several unique features that have been added to the basic system. In a broad aspect, the present invention provides a pyrolysis system where the system consists of two reactors. The horizontal reactor removes most of the volatile matter while the second, inclined auger reactor, allows for a longer contact time and removal of the remaining volatile matter under slow pyrolysis conditions.
In a broad aspect, then, the present invention relates to an apparatus for pyrolysis of organic material biomass, comprising: i) a first, horizontal auger tube having a first inlet for a heat carrier and a second inlet for biomass; and a first outlet for pyrolysis gas and a second outlet for said heat carrier and transformed biomass; and ii) a second, inclined auger tube having an inlet at or below the second outlet of said first auger tube, to receive the heat carrier and transformed biomass from the second outlet of the first auger tube and an outlet at a level above the inlet thereof, said outlet communicating with the first inlet of the first auger tube to deliver heat carrier thereto, wherein said heat carrier is steel shot.
DESCRIPTION OF THE DRAWINGS
Figure 1 is a schematic of the system of the present invention.
Figure 2a is a schematic of an auger tube with an auger having a fine pitch at one end and a coarser pitch at the other end.
Figure 2b is a schematic of an auger tube with an auger having a small effective carrying volume at one end, and a large effective carrying volume at the other end.
Figure 3 is a schematic of a char/shot separator used in a preferred embodiment of the present invention.
Figure 4 is a front view of an embodiment of the present invention.
Figure 5 is a rear view of the embodiment of the present invention shown in Figure 4, with the outer panels removed.
Referring first to the schematic diagram of Figure 1, the basic components of the pyrolysis apparatus of the present invention are shown. A first reactor comprises first tube 2 containing a screw conveyor comprising an auger. First tube 2 provided with a first inlet for steel shot, and a second inlet for biomass feed, downstream of the first inlet.
Steel shot with a temperature between 350 C and 550 C drops into the reactor conveyor tube (2). The level of shot is maintained higher than top elevation of the auger to ensure the auger is 100% full. The auger is turning at between 20 and 200 RPM with a preferred rotational speed of between 80 and 100 RPM. Feed enters the reactor from storage and can be conveyed to the reactor by an auger or series of augers or by any other means that will quickly introduce the biomass to the steel shot. The auger flighting pitch upstream of the feed entry point is set at 1/4 to 3/4 pitch, preferably 1/2 pitch. At the point of feed entry from (1) the pitch is increased to full or greater than full in such a manner that the shot level drops to approximately one¨half full. The increase in pitch assures space is available for the biomass in the auger and that there is head space above the shot and biomass to allow the gas to flow down the auger and out to a condenser. An alternate means of controlling the shot level in the reactor is to increase the auger shaft size upstream of the feed point and maintain full pitch throughout the entire auger length. The shaft at the feed entry point is a smaller diameter and therefore the shot level will drop. Figure 2a shows the half pitch auger while Figure 2b shows the larger shaft auger. Both of these methods have been tested by the Applicant and found to perform identically.
The hot pyrolysis gas exits the reactor downstream of the feed entry point and is conveyed by a system of pipes to a condensation unit (4) where the gas is cooled and the condensable materials are removed. The charcoal and shot continue past the gas exit point and drop into a second conveyor tube (3) containing a screw conveyor comprising an auger. The second conveyor tube is inclined upwardly relative to the first tube. The inclined conveyor tube provides a physical seal between the first reactor (2) and a charcoal recovery system (5) as will be discussed. Heat transfer through the shell of the inclined tube provides a means of heating the steel shot up to the desired temperature.
The temperature of the recycled steel shot is governed by the temperature external to the reactor and inclined auger shells. The mean reaction temperature is a function of the shot temperature and the mass ratio of steel shot to biomass. The temperature differential between the external temperature and the desired reaction temperature is a function of the type of biomass and its moisture content. Empirical observations have shown the biomass is rapidly mixed into the steel shot in two revolutions of the auger. Sixty to one hundred and twenty revolutions per minute for the reactor auger appear to be adequate to provide total incorporation of the biomass into the steel shot in a matter of 1 second.
Given the high thermal conductivity of steel shot and the rapid mixing, high liquid yields can be obtained for woody biomass within a temperature range of 350 C to 500 C. The preferred temperature is a function of the type of biomass, the amount of volatile matter to remain in the biochar, the desired liquid yield and the physical properties of the biomass. Circulating bed type reactors are known to have an optimum temperature of 515 C for similar biomass. Auger pyrolysis systems with a steel shot heat carrier are able to perform the same pyrolysis activity at a lower temperature and are hence more thermally efficient.
The heating of the charcoal in the second auger tube to a higher temperature than the primary reaction temperature can result in additional gas being produced. The amount of gas depends on the temperature of the shot following mixing with the biomass and the temperature to which the shot is heated in the inclined auger tube (3). At 400 C primary reaction temperature, more volatile matter remains in the char and hence more gas is produced during heating in the inclined auger. As discussed below, the charcoal recovery system (5) is isolated from the reactor system (2), and therefore an increase in pressure will occur in the charcoal recovery system if pressure relief isn't available.
Pressure relief is possible by allowing the excess gas to permeate through the shot at the entry point to the reaction auger tube (2). The size of the steel shot particles therefore is a factor in controlling pressure relief. If pyrolysis is conducted at 400 C and more gas is produced then the shot size has to be greater to allow for higher gas permeability. Steel shot with a grain size of 1 mm was found to be somewhat impervious to the excess gas given the length of the full section upstream of the feed entry point when the operating temperature was less than 450 C. Finer shot (1mm) can be used if the length of the full section is shortened. The choice of shot size and the geometry of the reactor can both be used to govern the pressure in the char recovery circuit.
The shot exits the inclined tube and drops down a chute to a char/shot separator (5). The separator (5) is a simple classifier device whose only moving part is a small radial fan blower (7). Recycle gas classification is possible because of the density difference between the shot and the char particles. Steel has a density of 7.3 g/cc while charcoal particles are reported to have particle densities in the range of 1.5 to 1.7 gm/cc. The steel shot acts as a ball mill and post pyrolysis charcoal has a grain size normally less than 1 mm.
Referring to Figure 3, the shot and char exit the upper end of the inclined auger tube and slide down an inclined plane and the combined mass drops over a step. Recycle gas from a blower (7) enters the separator from the back of the step and carries the char in the gas stream while the clean shot flows down an inclined plane and drops into a small surge bin at the start of the horizontal reactor tube (2). The charcoal is separated from the recycle gas stream via a cyclone (6). The charcoal exits the cyclone (6) and is conveyed to storage (8).
An advantage of the overall design of the system is in its compactness and simplicity. The reactor tube (2) and inclined tube (3) are located in parallel planes and the separator is small enough to fit between the two tubes. The apparatus has a small footprint per volume of biomass converted. Biooil yields of 70% have been measured. This yield is consistent with yields obtained by fluid bed and transport bed pyrolysis units. The simplicity and low capital cost and low operating cost per litre produced are unique to this invention.
Referring to Figure 5, it will be observed that all essential parts of the closed loop of the present apparatus, namely the reactor tube 2, the chute between reactor tube and the inclined tube 3, and the separator 5 that connects the top of the inclined tube with the steel shot input of the reactor tube, are all contained within a rectangular box-like structure. For clarity, the side walls of the box and heat source are not shown, but in operation, insulated walls, entirely enclose the box, creating an oven that can be maintained at a temperature suitable for conducting a pyrolysis reaction. Other portions of the system, such as the motors for turning the augers, and the hopper for biomass are located outside of the box.
Experimental Results Three tests were performed to demonstrate the validity of auger pyrolysis. In theory the lower the reactor temperature, the higher the char yield. The system of the present invention is designed to produce biooil and char is a by¨product. Normally the plant is operated with a reactor temperature between 450 C and 500 'C. In an attempt to maximize char yield the first test was run at 400 C.
The results of the three tests are shown in the summary table and graph that are provided below.
temperature biochar biooil gas 400 23.2 71.75 5.04 450 24.1 70.97 4.88 485 17.2 69.5 13.2 February 26, 27, 2013 70 _________________________________________ =
50 biochar ¨ 40 --=-- biooil 1-1-I 30 gas T-õ.õ.7 REACTOR TEMPERATURE (c) The key finding is the potential to conduct fast pyrolysis at temperatures in the low 400 C
range.
References 1) J. Lede Oil & Gas Science and Technology ¨ Rev. IFP Energies nouvelles Copyright 6 2013, IFP Energies nouvelles DOI: 10.2516/ogst/2013108 2) Brown, J.N. Development of a lab-scale auger reactor for biomass fast pyrolysis and process optimization using response surface methodology. M.S. thesis, Iowa State University, Ames, 2009.
3) Hornung et al. 2001 PLANT FOR THE THERMAL TREATMENT OF MATERIAL AND
OPERATION PROCESS THEREOF: EP 1354172 B1 3) Piskorz, Jan, Piotr Majerski, and Desmond Radlein, ENERGY EFFICIENT
LIQUEFACTION
4) A. Barry Freel RAPID THERMAL CONVERSION OF BIOMASS, CA 2705775 and Method and apparatus for a circulating bed transport fast pyrolysis reactor system
Hornung used hollow steel balls to rapidly pyrolyze biomass and separated the charcoal from the balls in a trommel screen. The balls were heated and circulated in a system of screw conveyors. This system has been used for a variety of applications and numerous papers have been written and patents filed on results from this process.
SUMMARY OF THE INVENTION
Auger pyrolysis has been shown above to be an improvement on the fluid bed and circulating bed pyrolysis systems. This invention is an improvement and simplification of the auger pyrolysis system developed by Fransham (2001). There are several unique features that have been added to the basic system. In a broad aspect, the present invention provides a pyrolysis system where the system consists of two reactors. The horizontal reactor removes most of the volatile matter while the second, inclined auger reactor, allows for a longer contact time and removal of the remaining volatile matter under slow pyrolysis conditions.
In a broad aspect, then, the present invention relates to an apparatus for pyrolysis of organic material biomass, comprising: i) a first, horizontal auger tube having a first inlet for a heat carrier and a second inlet for biomass; and a first outlet for pyrolysis gas and a second outlet for said heat carrier and transformed biomass; and ii) a second, inclined auger tube having an inlet at or below the second outlet of said first auger tube, to receive the heat carrier and transformed biomass from the second outlet of the first auger tube and an outlet at a level above the inlet thereof, said outlet communicating with the first inlet of the first auger tube to deliver heat carrier thereto, wherein said heat carrier is steel shot.
DESCRIPTION OF THE DRAWINGS
Figure 1 is a schematic of the system of the present invention.
Figure 2a is a schematic of an auger tube with an auger having a fine pitch at one end and a coarser pitch at the other end.
Figure 2b is a schematic of an auger tube with an auger having a small effective carrying volume at one end, and a large effective carrying volume at the other end.
Figure 3 is a schematic of a char/shot separator used in a preferred embodiment of the present invention.
Figure 4 is a front view of an embodiment of the present invention.
Figure 5 is a rear view of the embodiment of the present invention shown in Figure 4, with the outer panels removed.
Referring first to the schematic diagram of Figure 1, the basic components of the pyrolysis apparatus of the present invention are shown. A first reactor comprises first tube 2 containing a screw conveyor comprising an auger. First tube 2 provided with a first inlet for steel shot, and a second inlet for biomass feed, downstream of the first inlet.
Steel shot with a temperature between 350 C and 550 C drops into the reactor conveyor tube (2). The level of shot is maintained higher than top elevation of the auger to ensure the auger is 100% full. The auger is turning at between 20 and 200 RPM with a preferred rotational speed of between 80 and 100 RPM. Feed enters the reactor from storage and can be conveyed to the reactor by an auger or series of augers or by any other means that will quickly introduce the biomass to the steel shot. The auger flighting pitch upstream of the feed entry point is set at 1/4 to 3/4 pitch, preferably 1/2 pitch. At the point of feed entry from (1) the pitch is increased to full or greater than full in such a manner that the shot level drops to approximately one¨half full. The increase in pitch assures space is available for the biomass in the auger and that there is head space above the shot and biomass to allow the gas to flow down the auger and out to a condenser. An alternate means of controlling the shot level in the reactor is to increase the auger shaft size upstream of the feed point and maintain full pitch throughout the entire auger length. The shaft at the feed entry point is a smaller diameter and therefore the shot level will drop. Figure 2a shows the half pitch auger while Figure 2b shows the larger shaft auger. Both of these methods have been tested by the Applicant and found to perform identically.
The hot pyrolysis gas exits the reactor downstream of the feed entry point and is conveyed by a system of pipes to a condensation unit (4) where the gas is cooled and the condensable materials are removed. The charcoal and shot continue past the gas exit point and drop into a second conveyor tube (3) containing a screw conveyor comprising an auger. The second conveyor tube is inclined upwardly relative to the first tube. The inclined conveyor tube provides a physical seal between the first reactor (2) and a charcoal recovery system (5) as will be discussed. Heat transfer through the shell of the inclined tube provides a means of heating the steel shot up to the desired temperature.
The temperature of the recycled steel shot is governed by the temperature external to the reactor and inclined auger shells. The mean reaction temperature is a function of the shot temperature and the mass ratio of steel shot to biomass. The temperature differential between the external temperature and the desired reaction temperature is a function of the type of biomass and its moisture content. Empirical observations have shown the biomass is rapidly mixed into the steel shot in two revolutions of the auger. Sixty to one hundred and twenty revolutions per minute for the reactor auger appear to be adequate to provide total incorporation of the biomass into the steel shot in a matter of 1 second.
Given the high thermal conductivity of steel shot and the rapid mixing, high liquid yields can be obtained for woody biomass within a temperature range of 350 C to 500 C. The preferred temperature is a function of the type of biomass, the amount of volatile matter to remain in the biochar, the desired liquid yield and the physical properties of the biomass. Circulating bed type reactors are known to have an optimum temperature of 515 C for similar biomass. Auger pyrolysis systems with a steel shot heat carrier are able to perform the same pyrolysis activity at a lower temperature and are hence more thermally efficient.
The heating of the charcoal in the second auger tube to a higher temperature than the primary reaction temperature can result in additional gas being produced. The amount of gas depends on the temperature of the shot following mixing with the biomass and the temperature to which the shot is heated in the inclined auger tube (3). At 400 C primary reaction temperature, more volatile matter remains in the char and hence more gas is produced during heating in the inclined auger. As discussed below, the charcoal recovery system (5) is isolated from the reactor system (2), and therefore an increase in pressure will occur in the charcoal recovery system if pressure relief isn't available.
Pressure relief is possible by allowing the excess gas to permeate through the shot at the entry point to the reaction auger tube (2). The size of the steel shot particles therefore is a factor in controlling pressure relief. If pyrolysis is conducted at 400 C and more gas is produced then the shot size has to be greater to allow for higher gas permeability. Steel shot with a grain size of 1 mm was found to be somewhat impervious to the excess gas given the length of the full section upstream of the feed entry point when the operating temperature was less than 450 C. Finer shot (1mm) can be used if the length of the full section is shortened. The choice of shot size and the geometry of the reactor can both be used to govern the pressure in the char recovery circuit.
The shot exits the inclined tube and drops down a chute to a char/shot separator (5). The separator (5) is a simple classifier device whose only moving part is a small radial fan blower (7). Recycle gas classification is possible because of the density difference between the shot and the char particles. Steel has a density of 7.3 g/cc while charcoal particles are reported to have particle densities in the range of 1.5 to 1.7 gm/cc. The steel shot acts as a ball mill and post pyrolysis charcoal has a grain size normally less than 1 mm.
Referring to Figure 3, the shot and char exit the upper end of the inclined auger tube and slide down an inclined plane and the combined mass drops over a step. Recycle gas from a blower (7) enters the separator from the back of the step and carries the char in the gas stream while the clean shot flows down an inclined plane and drops into a small surge bin at the start of the horizontal reactor tube (2). The charcoal is separated from the recycle gas stream via a cyclone (6). The charcoal exits the cyclone (6) and is conveyed to storage (8).
An advantage of the overall design of the system is in its compactness and simplicity. The reactor tube (2) and inclined tube (3) are located in parallel planes and the separator is small enough to fit between the two tubes. The apparatus has a small footprint per volume of biomass converted. Biooil yields of 70% have been measured. This yield is consistent with yields obtained by fluid bed and transport bed pyrolysis units. The simplicity and low capital cost and low operating cost per litre produced are unique to this invention.
Referring to Figure 5, it will be observed that all essential parts of the closed loop of the present apparatus, namely the reactor tube 2, the chute between reactor tube and the inclined tube 3, and the separator 5 that connects the top of the inclined tube with the steel shot input of the reactor tube, are all contained within a rectangular box-like structure. For clarity, the side walls of the box and heat source are not shown, but in operation, insulated walls, entirely enclose the box, creating an oven that can be maintained at a temperature suitable for conducting a pyrolysis reaction. Other portions of the system, such as the motors for turning the augers, and the hopper for biomass are located outside of the box.
Experimental Results Three tests were performed to demonstrate the validity of auger pyrolysis. In theory the lower the reactor temperature, the higher the char yield. The system of the present invention is designed to produce biooil and char is a by¨product. Normally the plant is operated with a reactor temperature between 450 C and 500 'C. In an attempt to maximize char yield the first test was run at 400 C.
The results of the three tests are shown in the summary table and graph that are provided below.
temperature biochar biooil gas 400 23.2 71.75 5.04 450 24.1 70.97 4.88 485 17.2 69.5 13.2 February 26, 27, 2013 70 _________________________________________ =
50 biochar ¨ 40 --=-- biooil 1-1-I 30 gas T-õ.õ.7 REACTOR TEMPERATURE (c) The key finding is the potential to conduct fast pyrolysis at temperatures in the low 400 C
range.
References 1) J. Lede Oil & Gas Science and Technology ¨ Rev. IFP Energies nouvelles Copyright 6 2013, IFP Energies nouvelles DOI: 10.2516/ogst/2013108 2) Brown, J.N. Development of a lab-scale auger reactor for biomass fast pyrolysis and process optimization using response surface methodology. M.S. thesis, Iowa State University, Ames, 2009.
3) Hornung et al. 2001 PLANT FOR THE THERMAL TREATMENT OF MATERIAL AND
OPERATION PROCESS THEREOF: EP 1354172 B1 3) Piskorz, Jan, Piotr Majerski, and Desmond Radlein, ENERGY EFFICIENT
LIQUEFACTION
4) A. Barry Freel RAPID THERMAL CONVERSION OF BIOMASS, CA 2705775 and Method and apparatus for a circulating bed transport fast pyrolysis reactor system
5) Fransham, Peter PROCESS FOR THE CONVERSION OF CARBONACEOUS
FEEDSTOCK INTO LIQUID, CHAR AND GAS CA 2351892
FEEDSTOCK INTO LIQUID, CHAR AND GAS CA 2351892
Claims (5)
1. An apparatus for pyrolysis of organic material biomass, comprising:
i) a first, horizontal auger tube having a first inlet for a heat carrier and a second inlet for biomass; and a first outlet for pyrolysis gas and a second outlet for said heat carrier and transformed biomass; and ii) a second, inclined auger tube having an inlet at or below the second outlet of said first auger tube, to receive the heat carrier and transformed biomass from the second outlet of the first auger tube and an outlet at a level above the inlet thereof, said outlet communicating with the first inlet of the first auger tube to deliver heat carrier thereto, wherein said heat carrier is steel shot.
i) a first, horizontal auger tube having a first inlet for a heat carrier and a second inlet for biomass; and a first outlet for pyrolysis gas and a second outlet for said heat carrier and transformed biomass; and ii) a second, inclined auger tube having an inlet at or below the second outlet of said first auger tube, to receive the heat carrier and transformed biomass from the second outlet of the first auger tube and an outlet at a level above the inlet thereof, said outlet communicating with the first inlet of the first auger tube to deliver heat carrier thereto, wherein said heat carrier is steel shot.
2. An apparatus as claimed in claim 1, wherein said outlet of said second auger is connected to the first inlet of said first auger tube via a classifier, whereby transformed biomass and steel shot exiting from the outlet of said second auger tube travels down an inclined chute and transformed biomass is separated from said steel shot by a flow of recycled gas, that carries the transformed biomass to a cyclone for separation from the recycled gas and permits the steel shot to continue down the chute to the inlet of the first auger.
3. An apparatus as claimed in clam 2, wherein said chute is intersected by a first conduit for recycled gas, and the intersection of the first conduit and the chute defines a step over which the steel shot and transformed biomass will fall, so that the recycled gas can separate the transformed biomass from the steel shot, and carry it, via a second conduit aligned with the first conduit, to said cyclone.
4. Apparatus as claimed in claim 2 or 3, wherein the pitch or carrying capacity of said first auger between said first inlet and said second inlet is less than the pitch or carrying capacity of said auger between said second inlet and said second outlet.
5. Apparatus as claimed in claim 3 or 4, wherein the first auger tube, second auger tube, first and second conduits, and cyclone form a closed loop.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA2821474A CA2821474C (en) | 2013-07-19 | 2013-07-19 | Compact fast pyrolysis system for conversion of carbonacous materials to liquid, solid and gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA2821474A CA2821474C (en) | 2013-07-19 | 2013-07-19 | Compact fast pyrolysis system for conversion of carbonacous materials to liquid, solid and gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2821474A1 CA2821474A1 (en) | 2015-01-19 |
| CA2821474C true CA2821474C (en) | 2018-05-01 |
Family
ID=52471789
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2821474A Active CA2821474C (en) | 2013-07-19 | 2013-07-19 | Compact fast pyrolysis system for conversion of carbonacous materials to liquid, solid and gas |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA2821474C (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AT519471B1 (en) * | 2017-02-06 | 2018-07-15 | Herz Energietechnik Gmbh | Verkohlungsanlage |
-
2013
- 2013-07-19 CA CA2821474A patent/CA2821474C/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CA2821474A1 (en) | 2015-01-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Qureshi et al. | A technical review on semi-continuous and continuous pyrolysis process of biomass to bio-oil | |
| JP5925195B2 (en) | Method and system for crushing pyrolysis of particulate carbonaceous feedstock | |
| Ellens et al. | Optimization of a free-fall reactor for the production of fast pyrolysis bio-oil | |
| EP1235886B1 (en) | Flash-pyrolysis in a cyclone | |
| US10041667B2 (en) | Apparatuses for controlling heat for rapid thermal processing of carbonaceous material and methods for the same | |
| CN107189799B (en) | Material co-pyrolysis reaction system and pyrolysis method | |
| US4539917A (en) | Combustion heater for oil shale | |
| JP5407496B2 (en) | Fluidized bed drying and heating classifier and co-coking coal pretreatment method | |
| US20150021159A1 (en) | Compact fast pyrolysis system for conversion of carbonaceous materials to liquid, solid and gas | |
| CA2821474C (en) | Compact fast pyrolysis system for conversion of carbonacous materials to liquid, solid and gas | |
| JP3322338B2 (en) | Charcoal and activated carbon production equipment | |
| CN103267405B (en) | Coal drying device and drying means | |
| US10513660B2 (en) | Compact fast pyrolysis system for conversion of carbonaceous materials to liquid, solid and gas | |
| Guoxin et al. | Experimental studies on flow and pyrolysis of coal with solid heat carrier in a modified rotating cone reactor | |
| CN103265961B (en) | Carbon species method for pyrolysis and carbon substance vibration pyrolysis tower | |
| Rojcewicz et al. | Modification of fountain bed dryer for sawdust drying for fuel pellets production | |
| US2773018A (en) | Continuous process for drying, preheating, and devolatilization of carbonaceous materials | |
| US20090045103A1 (en) | Thermal coal upgrading process | |
| CN206887028U (en) | Material copyrolysis reaction system | |
| CN101479028B (en) | A horizontal fluidised bed reactor | |
| CN206204224U (en) | A kind of low temperature continuous pyrolysis process useless circuit board fixed bed reactors | |
| JP2001233610A (en) | Production arrangement for charcoal and activated carbon | |
| JP2014159001A (en) | Raw material feeding device and method, and fluid bed dryer | |
| US11873450B2 (en) | Systems and methods for the thermochemical production and refining of hydrocarbon compounds | |
| US20230038042A1 (en) | Pyrolysis system, a method for producing purified pyrolysis gas and pyrolysis liquids and use of a pyrolysis system |