CA2351892C - Process for the conversion of carbonaceous feedstock into liquid, char and gas - Google Patents
Process for the conversion of carbonaceous feedstock into liquid, char and gas Download PDFInfo
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- CA2351892C CA2351892C CA002351892A CA2351892A CA2351892C CA 2351892 C CA2351892 C CA 2351892C CA 002351892 A CA002351892 A CA 002351892A CA 2351892 A CA2351892 A CA 2351892A CA 2351892 C CA2351892 C CA 2351892C
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- Prior art keywords
- carbonaceous feedstock
- pyrolytic
- reactor tube
- char
- feedstock
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Classifications
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- 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
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/28—Other processes
- C10B47/32—Other processes in ovens with mechanical conveying means
- C10B47/44—Other processes in ovens with mechanical conveying means 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
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- 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
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
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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
Abstract
The invention relates to a process for the pyrolytic conversion of carbonaceous waste materials into liquids, char, and gas which may be used as fuel or as a source of chemical feedstocks. Carbonaceous feedstock is heated and may be mixed with heated inert particulate material, with the resulting pyrolytic gases being cooled and condensed by passage through a condenser and a venturi scrubber. The process is energy efficient, and produces good yields of high quality pyrolytic liquids at relatively low temperatures. By varying the reactor temperature it is possible to vary the percentage of liquid, char, and gas produced. The process can be optimized to produce maximum yields of the three major by-products.
Description
PROCESS FOR THE CONVERSION OF CARBONACEOUS FEEDSTOCK INTO
LIQUID, CHAR, AND GAS
Field of the Invention This invention relates to a process for the pyrolytic conversion of carbonaceous materials into liquid, char, and gas. The process improves upon current practices by eliminating the need for a blower and cyclone to circulate gas, thus significantly reducing energy requirements. In addition, the process results in a relatively high yield of good quality pyrolytic liquids at temperatures lower than those reported by others.
Background to the Invention Pyrolysis is the decomposition of compounds caused by rapid heating in an oxygen-depleted environment. The process may be used to derive fuel oils from a number of carbonaceous materials. The wood or forest products industry produces sawdust, wood chips, bark, construction debris, and post consumer wood waste. The agricultural sector has abundant supplies of straw, hay, wood crop grown specifically for energy, and manure.
Miscellaneous wastes consisting of tires, plastic, and treated wood may also be converted into value-added fuels and chemicals. Greater yields of pyrolytic oils are produced where the time between thermal decomposition and condensation is minimized, the ideal time being in the order of a few seconds. U.S. Patent No. 5,853,548 to Piskorz et al. shows that the requirement for short residence time decreases as the temperature decreases.
LIQUID, CHAR, AND GAS
Field of the Invention This invention relates to a process for the pyrolytic conversion of carbonaceous materials into liquid, char, and gas. The process improves upon current practices by eliminating the need for a blower and cyclone to circulate gas, thus significantly reducing energy requirements. In addition, the process results in a relatively high yield of good quality pyrolytic liquids at temperatures lower than those reported by others.
Background to the Invention Pyrolysis is the decomposition of compounds caused by rapid heating in an oxygen-depleted environment. The process may be used to derive fuel oils from a number of carbonaceous materials. The wood or forest products industry produces sawdust, wood chips, bark, construction debris, and post consumer wood waste. The agricultural sector has abundant supplies of straw, hay, wood crop grown specifically for energy, and manure.
Miscellaneous wastes consisting of tires, plastic, and treated wood may also be converted into value-added fuels and chemicals. Greater yields of pyrolytic oils are produced where the time between thermal decomposition and condensation is minimized, the ideal time being in the order of a few seconds. U.S. Patent No. 5,853,548 to Piskorz et al. shows that the requirement for short residence time decreases as the temperature decreases.
2 Most pyrolysis reactors are of the fluidized bed, circulating fluidized bed or transport bed type (see, for example, Canadian Patent No. 2,150,231 to Scott et al. and Canadian Patent No. 982,073 to Garrett and Mallan). In each of these reactor types, termed circulating gas pyrolysis systems, heating of the carbonaceous material is accomplished, at least in part, by mixing the carbonaceous material with a hot, inert substance. The inert substance always consists of gaseous materials, but solids may also be present. The inert gas, along with any products of the pyrolysis reaction, is directed out of the reactor by a recycle gas stream produced by a blower. The recycle gas stream flows into a cyclone, where the char is separated out. Next, the pyrolytic oils are isolated by condensation. The inert gas is then reheated and cycled back to the reactor. The presence of this recycle gas stream not only increases the size and complexity of the pyrolysis system, but it increases the size of the condensing system and, due to continual heating and cooling of the recycle gas, greatly increases the energy requirements of the system. Additionally, the amount of recycle gas becomes so great that a larger cyclone is required, thus increasing the time between thermal decomposition and condensation.
A further difficulty with circulating gas pyrolysis systems is the condensation of vapours.
Despite the presence of condensers, filters and demisters are normally required, and the latter may trap as much as half of the pyrolytic oils. This necessitates frequent draining and servicing of filters and demisters.
Optimum pyrolysis temperatures in the prior art are in the range of 500 C for a circulating bed transport reactor (U.S. Patent No. 5,961,786 to Freel and Graham), and Piskorz et al.
have reported a preferred temperature of 430 C in a fluidized bed reactor (U.S. Patent No.
5,853,548).
There have been attempts to use auger systems as pyrolysis reactors (U.S.
Patent No.
4,983,278 to Cha et al., and U.S. Patent No. 5,720,232 to Meador). These reactors were designed primarily for the recovery of oil from tar sands and tires, and are slow pyrolysis systems with limited product throughput. In H.W. Campbell "Converting Sludge to Fuel - A
Status Report" in Hogan et al eds., Biomass Thermal Processing, (Berkshire, UK: CPL
Press Newbury, 1992) at 78-84, Campbell describes a heated auger and gas flow process for the conversion of sludge to fuel. This system produced lower liquid yield and higher char yield than the present invention as claimed.
A further difficulty with circulating gas pyrolysis systems is the condensation of vapours.
Despite the presence of condensers, filters and demisters are normally required, and the latter may trap as much as half of the pyrolytic oils. This necessitates frequent draining and servicing of filters and demisters.
Optimum pyrolysis temperatures in the prior art are in the range of 500 C for a circulating bed transport reactor (U.S. Patent No. 5,961,786 to Freel and Graham), and Piskorz et al.
have reported a preferred temperature of 430 C in a fluidized bed reactor (U.S. Patent No.
5,853,548).
There have been attempts to use auger systems as pyrolysis reactors (U.S.
Patent No.
4,983,278 to Cha et al., and U.S. Patent No. 5,720,232 to Meador). These reactors were designed primarily for the recovery of oil from tar sands and tires, and are slow pyrolysis systems with limited product throughput. In H.W. Campbell "Converting Sludge to Fuel - A
Status Report" in Hogan et al eds., Biomass Thermal Processing, (Berkshire, UK: CPL
Press Newbury, 1992) at 78-84, Campbell describes a heated auger and gas flow process for the conversion of sludge to fuel. This system produced lower liquid yield and higher char yield than the present invention as claimed.
3 Object and Summary of the Invention An object of the invention is to provide a process with improved energy efficiency and reduced financial cost for the pyrolytic liquidation of carbonaceous feedstock.
A further object of the invention is to provide a flexible process for the pyrolytic liquidation or gasification of carbonaceous feedstock to produce better quality pyrolytic oils and/or combustible gas.
Broadly, this invention relates to a process for the conversion of hydrocarbon feedstock into pyrolytic liquid, char and gas, comprising the following: introducing carbonaceous feedstock, through an inlet means, into a pyrolytic reactor tube wherein said carbonaceous feedstock is moved through said pyrolytic reactor tube by a rotating auger;
heating said feedstock in said reactor tube by mixing said feedstock with a heated inert particulate material, causing the pyrolysis of said carbonaceous feedstock, and resulting in solid product and gaseous product; discharging said solid product through an outlet means;
discharging said gaseous product through a second outlet means; and cooling and condensing said gaseous product in a series of condensers, said series of condensers comprising at least one venturi scrubber.
In the case where the throughput is five (5) tonnes per day or less, the requirement for a heated inert particulate material can be eliminated. The hot pyrolytic reactor tube provides sufficient heat transfer to rapidly convert the carbonaceous material to liquid, solid and gas.
Detailed Description of the Invention The applicant's invention is designed to overcome the drawbacks listed above.
Briefly, the invention relates to a process whereby carbonaceous feedstock is directed from a storage hopper, by virtue of a rotating feed auger, into a pyrolytic reactor tube, which houses a rotating auger. An external heat source heats the pyrolytic reactor tube, and a heated solid inert particulate material, such as steel shot, may be mixed with the carbonaceous feedstock. Pyrolysis occurs at a temperature of approximately 400 C. Solid materials (char and inert particulate material when required) exit the pyrolytic reactor tube and are separated. The inert particulate material may be reheated and reused, while the char may be combusted. The heat provided by combustion of the char is used to heat the pyrolytic
A further object of the invention is to provide a flexible process for the pyrolytic liquidation or gasification of carbonaceous feedstock to produce better quality pyrolytic oils and/or combustible gas.
Broadly, this invention relates to a process for the conversion of hydrocarbon feedstock into pyrolytic liquid, char and gas, comprising the following: introducing carbonaceous feedstock, through an inlet means, into a pyrolytic reactor tube wherein said carbonaceous feedstock is moved through said pyrolytic reactor tube by a rotating auger;
heating said feedstock in said reactor tube by mixing said feedstock with a heated inert particulate material, causing the pyrolysis of said carbonaceous feedstock, and resulting in solid product and gaseous product; discharging said solid product through an outlet means;
discharging said gaseous product through a second outlet means; and cooling and condensing said gaseous product in a series of condensers, said series of condensers comprising at least one venturi scrubber.
In the case where the throughput is five (5) tonnes per day or less, the requirement for a heated inert particulate material can be eliminated. The hot pyrolytic reactor tube provides sufficient heat transfer to rapidly convert the carbonaceous material to liquid, solid and gas.
Detailed Description of the Invention The applicant's invention is designed to overcome the drawbacks listed above.
Briefly, the invention relates to a process whereby carbonaceous feedstock is directed from a storage hopper, by virtue of a rotating feed auger, into a pyrolytic reactor tube, which houses a rotating auger. An external heat source heats the pyrolytic reactor tube, and a heated solid inert particulate material, such as steel shot, may be mixed with the carbonaceous feedstock. Pyrolysis occurs at a temperature of approximately 400 C. Solid materials (char and inert particulate material when required) exit the pyrolytic reactor tube and are separated. The inert particulate material may be reheated and reused, while the char may be combusted. The heat provided by combustion of the char is used to heat the pyrolytic
4 reactor tube and the inert particulate material (if present). Gaseous material exits the pyrolytic reactor tube and is cooled and condensed in a primary condenser, consisting of a cooled tubular shell or a venturi scrubber followed by a polishing venturi scrubber.
Uncondensed gaseous material may be passed through a demister and filter.
This invention eliminates the need for a blower and cyclone, thereby decreasing the size of the system and increasing energy efficiency. Because char is mechanically conveyed directly from the reactor, separately from gaseous materials, a large cyclone is unnecessary.
Furthermore, gas produced from the pyrolysis reaction is swept from the reactor within less than approximately one or two seconds. This is accomplished without the need for a blower, as the downstream venturi scrubber(s) and the increasing gas pressure within the reactor create a pressure differential which forces the pyrolysis gas out of the reactor. A further advantage is that because the system acts with virtually zero pressure, it is not subject to strict ASME fabrication codes regulating pressure vessels, meaning that the system is less expensive to manufacture.
Condensation difficulties in circulating gas pyrolysis systems are believed to be caused by the atomization of pyrolysis gases by the high circulating gas flow. The atomization prevents condensation from occurring. The elimination of a recycle gas flow in this invention has led to better condensation. In a full-sized reactor, the need for a filter and demister may be entirely eliminated, due to virtually 100% condensation in the primary and venturi condensers. Tests to date have shown that only 1.5% of the condensable liquids are recovered in the demister and filter.
It was discovered that with the heated auger reactor, maximum liquid yields were obtained at a temperature slightly under 400 C, and excellent yields were obtained over the range of 380 C to 420 C. These temperatures are quite low, meaning that the system may be operated at a lower cost due to lower energy requirements. Furthermore, a lower operating temperature reduces the need for expensive process parts m,made from stainless steel.
It was also discovered that with the heated auger reactor, maximum gas yields were obtained at a temperature above 500 C. At this temperature there is a need for more expensive process parts from stainless steel.
An additional advantage of the low operating temperature is an improved quality of pyrolytic oils. At temperatures above 360 C, pyrolytic oils are relatively unstable, and will undergo secondary reactions which decrease the quality of the pyrolytic oils. It is therefore crucial to minimize the time at which the pyrolytic oils are at a temperature above 360 C. An optimum temperature of 400 C will decrease the likelihood of secondary reactions and decrease the importance of a short time between thermal decomposition and cooling below 360 C.
In fact, the pyrolytic oils obtained were in a single phase, and with a moisture content of nearly 40% . These are both positive qualities, as a single phase oil may be pumped directly into an engine without preheating, while water content helps to reduce NOX
emissions, and to atomize the oil, thus allowing for better combustion. Lower pyrolysis temperature is thought to allow for the preservation of bridging compounds which allow the oil and water to maintain a single phase, even where water content is relatively high.
Description of the Drawings In drawings that illustrate the present invention by way of example:
Figure 1 is a schematic drawing of one embodiment of the process of the invention.
Figure 2 is a schematic drawing a second embodiment of the process of the invention.
Figure 1 illustrates a preferred embodiment of the process of the invention.
In this embodiment, the carbonaceous feedstock is fed into a storage hopper (1). The carbonaceous feedstock is directed from the storage hopper (1) by virtue of a rotating feed auger (2). The carbonaceous feedstock enters an open chamber in a hydraulic ram (3) and is compressed by the ram. From the hydraulic ram the feedstock enters a second rotating feed auger (4). From the second rotating feed auger (4), the carbonaceous feedstock enters the pyrolytic reactor tube (5), which houses a rotating auger (6).
Solid materials exit the pyrolytic reactor tube via the solids exit tube (7), and are directed towards a rotating transfer auger (8). Solids are then transferred via a bucket elevator (9) to a rotating separation auger (10). Char is separated out from inert particulate material, and funnelled off to a lock hopper (11) for storage. The inert particulate material is heated in a heater (12) and directed through a rotating feed auger (13) to the rotating feed auger (4) which leads back to the pyrolytic reactor tube (5). Gaseous material departs the pyrolytic reactor tube
Uncondensed gaseous material may be passed through a demister and filter.
This invention eliminates the need for a blower and cyclone, thereby decreasing the size of the system and increasing energy efficiency. Because char is mechanically conveyed directly from the reactor, separately from gaseous materials, a large cyclone is unnecessary.
Furthermore, gas produced from the pyrolysis reaction is swept from the reactor within less than approximately one or two seconds. This is accomplished without the need for a blower, as the downstream venturi scrubber(s) and the increasing gas pressure within the reactor create a pressure differential which forces the pyrolysis gas out of the reactor. A further advantage is that because the system acts with virtually zero pressure, it is not subject to strict ASME fabrication codes regulating pressure vessels, meaning that the system is less expensive to manufacture.
Condensation difficulties in circulating gas pyrolysis systems are believed to be caused by the atomization of pyrolysis gases by the high circulating gas flow. The atomization prevents condensation from occurring. The elimination of a recycle gas flow in this invention has led to better condensation. In a full-sized reactor, the need for a filter and demister may be entirely eliminated, due to virtually 100% condensation in the primary and venturi condensers. Tests to date have shown that only 1.5% of the condensable liquids are recovered in the demister and filter.
It was discovered that with the heated auger reactor, maximum liquid yields were obtained at a temperature slightly under 400 C, and excellent yields were obtained over the range of 380 C to 420 C. These temperatures are quite low, meaning that the system may be operated at a lower cost due to lower energy requirements. Furthermore, a lower operating temperature reduces the need for expensive process parts m,made from stainless steel.
It was also discovered that with the heated auger reactor, maximum gas yields were obtained at a temperature above 500 C. At this temperature there is a need for more expensive process parts from stainless steel.
An additional advantage of the low operating temperature is an improved quality of pyrolytic oils. At temperatures above 360 C, pyrolytic oils are relatively unstable, and will undergo secondary reactions which decrease the quality of the pyrolytic oils. It is therefore crucial to minimize the time at which the pyrolytic oils are at a temperature above 360 C. An optimum temperature of 400 C will decrease the likelihood of secondary reactions and decrease the importance of a short time between thermal decomposition and cooling below 360 C.
In fact, the pyrolytic oils obtained were in a single phase, and with a moisture content of nearly 40% . These are both positive qualities, as a single phase oil may be pumped directly into an engine without preheating, while water content helps to reduce NOX
emissions, and to atomize the oil, thus allowing for better combustion. Lower pyrolysis temperature is thought to allow for the preservation of bridging compounds which allow the oil and water to maintain a single phase, even where water content is relatively high.
Description of the Drawings In drawings that illustrate the present invention by way of example:
Figure 1 is a schematic drawing of one embodiment of the process of the invention.
Figure 2 is a schematic drawing a second embodiment of the process of the invention.
Figure 1 illustrates a preferred embodiment of the process of the invention.
In this embodiment, the carbonaceous feedstock is fed into a storage hopper (1). The carbonaceous feedstock is directed from the storage hopper (1) by virtue of a rotating feed auger (2). The carbonaceous feedstock enters an open chamber in a hydraulic ram (3) and is compressed by the ram. From the hydraulic ram the feedstock enters a second rotating feed auger (4). From the second rotating feed auger (4), the carbonaceous feedstock enters the pyrolytic reactor tube (5), which houses a rotating auger (6).
Solid materials exit the pyrolytic reactor tube via the solids exit tube (7), and are directed towards a rotating transfer auger (8). Solids are then transferred via a bucket elevator (9) to a rotating separation auger (10). Char is separated out from inert particulate material, and funnelled off to a lock hopper (11) for storage. The inert particulate material is heated in a heater (12) and directed through a rotating feed auger (13) to the rotating feed auger (4) which leads back to the pyrolytic reactor tube (5). Gaseous material departs the pyrolytic reactor tube
(5) via the gas exit tube (14) and is directed to a primary condenser (15) which is run using a primary cooling pump (16). From the primary condenser (23), uncondensed gaseous material is directed to a venturi condenser (16) which is run using a secondary cooling pump (24). Condensed liquids are collected by virtue of a liquid transfer pump (18). -Figure 2 illustrates a preferred embodiment of the process of the invention for systems with less than 5 tonnes of throughput per day. In this embodiment, the carbonaceous feedstock is fed into a storage, hopper (1). The carbonaceous feedstock is directed from the storage hopper (1) by a rotating feed auger (2). The carbonaceous feedstock enters an open chamber in the reciprocating ram (3) and is compressed by the ram (3). From the reciprocating ram (3), the carbonaceous feedstock enters a rotating feed auger (4) and is conveyed to the pyrolytic reactor tube (5), which houses a rotating auger (6).
Char exits the pyrolytic reactor tube (5) via the solids exit tube (7), and is directed towards a lock hopper (11). Char is then combusted in a fluid bed furnace (29). Fluidization and combustion air are provided by a blower (25) and the residual solid ash is separated from the combustion gas via a cyclonic separator (26). The ash is directed through a rotary air lock (27) to an ash storage bin (28). The cleansed combustion gas is directed out of the cyclone via an exit tube (30) and the hot combustion gas circulates around the rotating auger shell (6) and heats the pyrolytic reactor tube (5). Gaseous material departs the pyrolytic reactor tube (5) via the gas exit tube (14) and is directed to a primary venturi condenser (15) which is run using a primary cooling pump (16). Fluids pumped by the primary cooling pump (16) are cooled by a heat exchanger (17) prior to entering the primary condenser (15).
From the primary condenser (15), uncondensed gaseous material is directed to a secondary venturi condenser (23) which is run using a secondary cooling pump (24) and a heat exchanger (20). Condensed liquids are transferred to storage tanks by a liquid transfer pump (18).
Non-condensing gases are directed out of the secondary venturi scrubber to a flare stack (22).
The examples and embodiments described herein are for illustrative purposes only, and are not meant to limit the scope of the invention. Various modifications or changes will be suggested to persons skilled in the art, and are to be included within the spirit and purview of this applications and the scope of the appended claims.
Example 1 Oak sawdust was subjected to pyrolysis at 431 C with a feed rate of 0.76 kg/h and a rotating auger speed of 2.0 rpm, resulting in the following yields:
Liquid: 46.9%
Char: 26.0%
Gas: 27.0%
Example 2 Oak sawdust was subjected to pyrolysis at 391 C with a feed rate of 0.80 kg/h and a rotating auger speed of 2.0 rpm, resulting in the following yields:
Liquid: 54.1%
Char: 21.6%
Gas: 24.3%
Example 3 Oak sawdust was subjected to pyrolysis at 349 C with a feed rate of 1.04 kg/h and a rotating auger speed of 2.0 rpm, resulting in the following yields:
Liquid: 51.7%
Char: 28.9%
Gas: 19.4%
Example 4 Pine sawdust was subjected to pyrolysis at 406 C with a feed rate of 1.4 kg/h and a rotating auger speed of 2.0 rpm, resulting in the following yields:
Liquid: 58.0%
Char: 33.0%
Gas: 8.7%
Example 5 Pine sawdust was subjected to pyrolysis at 390 C with a fe d rate of 1.4 kg/h and a rotating auger speed of 2.0 rpm, resulting in the following yields:
Liquid: 57%
Char: 25%
Gas: 8%
Example 6 Chicken manure was subjected to pyrolysis at 399 C with a feed rate of 2.2 kg/h and a rotating auger speed of 2.0 rpm, resulting in the following yieIds:
Light liquid: 29%
Heavy liquid: 10%
Char: 40%
Gas: 21%
Char exits the pyrolytic reactor tube (5) via the solids exit tube (7), and is directed towards a lock hopper (11). Char is then combusted in a fluid bed furnace (29). Fluidization and combustion air are provided by a blower (25) and the residual solid ash is separated from the combustion gas via a cyclonic separator (26). The ash is directed through a rotary air lock (27) to an ash storage bin (28). The cleansed combustion gas is directed out of the cyclone via an exit tube (30) and the hot combustion gas circulates around the rotating auger shell (6) and heats the pyrolytic reactor tube (5). Gaseous material departs the pyrolytic reactor tube (5) via the gas exit tube (14) and is directed to a primary venturi condenser (15) which is run using a primary cooling pump (16). Fluids pumped by the primary cooling pump (16) are cooled by a heat exchanger (17) prior to entering the primary condenser (15).
From the primary condenser (15), uncondensed gaseous material is directed to a secondary venturi condenser (23) which is run using a secondary cooling pump (24) and a heat exchanger (20). Condensed liquids are transferred to storage tanks by a liquid transfer pump (18).
Non-condensing gases are directed out of the secondary venturi scrubber to a flare stack (22).
The examples and embodiments described herein are for illustrative purposes only, and are not meant to limit the scope of the invention. Various modifications or changes will be suggested to persons skilled in the art, and are to be included within the spirit and purview of this applications and the scope of the appended claims.
Example 1 Oak sawdust was subjected to pyrolysis at 431 C with a feed rate of 0.76 kg/h and a rotating auger speed of 2.0 rpm, resulting in the following yields:
Liquid: 46.9%
Char: 26.0%
Gas: 27.0%
Example 2 Oak sawdust was subjected to pyrolysis at 391 C with a feed rate of 0.80 kg/h and a rotating auger speed of 2.0 rpm, resulting in the following yields:
Liquid: 54.1%
Char: 21.6%
Gas: 24.3%
Example 3 Oak sawdust was subjected to pyrolysis at 349 C with a feed rate of 1.04 kg/h and a rotating auger speed of 2.0 rpm, resulting in the following yields:
Liquid: 51.7%
Char: 28.9%
Gas: 19.4%
Example 4 Pine sawdust was subjected to pyrolysis at 406 C with a feed rate of 1.4 kg/h and a rotating auger speed of 2.0 rpm, resulting in the following yields:
Liquid: 58.0%
Char: 33.0%
Gas: 8.7%
Example 5 Pine sawdust was subjected to pyrolysis at 390 C with a fe d rate of 1.4 kg/h and a rotating auger speed of 2.0 rpm, resulting in the following yields:
Liquid: 57%
Char: 25%
Gas: 8%
Example 6 Chicken manure was subjected to pyrolysis at 399 C with a feed rate of 2.2 kg/h and a rotating auger speed of 2.0 rpm, resulting in the following yieIds:
Light liquid: 29%
Heavy liquid: 10%
Char: 40%
Gas: 21%
Claims (16)
PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for the conversion of hydrocarbon feedstock into pyrolytic liquid, char and gas, comprising the following:
introducing carbonaceous feedstock, through an inlet means, into a pyrolytic reactor tube wherein said carbonaceous feedstock is moved through said pyrolytic reactor tube by a rotating auger;
heating said feedstock in said reactor tube by mixing said feedstock with a heated inert particulate material, causing the pyrolysis of said carbonaceous feedstock, and resulting in solid product and gaseous product;
discharging said solid product through an outlet means;
discharging said gaseous product through a second outlet means; and cooling and condensing said gaseous product in a series of condensers, said series of condensers comprising at least one venturi scrubber.
introducing carbonaceous feedstock, through an inlet means, into a pyrolytic reactor tube wherein said carbonaceous feedstock is moved through said pyrolytic reactor tube by a rotating auger;
heating said feedstock in said reactor tube by mixing said feedstock with a heated inert particulate material, causing the pyrolysis of said carbonaceous feedstock, and resulting in solid product and gaseous product;
discharging said solid product through an outlet means;
discharging said gaseous product through a second outlet means; and cooling and condensing said gaseous product in a series of condensers, said series of condensers comprising at least one venturi scrubber.
2. A process as claimed in claim 1, wherein said inert particulate material is steel shot.
3. A process as claimed in claim 2, wherein said carbonaceous feedstock is selected from a group consisting of sawdust, wood chips, wood shavings, bark, construction debris, post consumer wood waste, straw, hay, manure, chicken litter, bagasse, tires, tire crumb, plastic, and treated wood.
4. A process as claimed in claim 2 or 3, wherein said inlet means consists of:
a storage means for said carbonaceous feedstock;
a rotating auger, which directs said carbonaceous feedstock out of said storage means; and a reciprocating ram, which compresses said carbonaceous feedstock and directs said carbonaceous feedstock into said pyrolytic reactor tube.
a storage means for said carbonaceous feedstock;
a rotating auger, which directs said carbonaceous feedstock out of said storage means; and a reciprocating ram, which compresses said carbonaceous feedstock and directs said carbonaceous feedstock into said pyrolytic reactor tube.
5. A process as claimed in claim 4, wherein said compression of carbonaceous feedstock forms a plug, preventing flow of pyrolysis products out of said pyrolytic reactor tube through said inlet means.
6. A process as claimed in claim 5, wherein the backstroke of said hydraulic ram causes some oxygen free pyrolysis vapours to be drawn into said carbonaceous feedstock plug, displacing air from said pyrolytic reactor.
7. A process as claimed in claim 6, wherein said rotating auger in said pyrolytic reactor tube is driven by a hydraulic or electric motor.
8. A process as claimed in any of claims 2, 3, 4, 5, 6 or 7, wherein said steel shot consists of steel spheres with a diameter of less than 1 centimetre.
9. A process as claimed in any of claims 2, 3, 4, 5, 6, 7 or 8, wherein the temperature inside said pyrolytic reactor tube is in the range of 350°C to 550°C.
10. A process as claimed in any of claims 2, 3, 4, 5, 6, 7, 8 or 9, wherein the residence time of said carbonaceous feedstock inside said pyrolytic reactor tube is less than 10 minutes.
11. A process as claimed in any of claims 2, 3, 4, 5, 6, 7, 8, 9 or 10, wherein said solid material is comprised of char and inert particulate material.
12. A process as claimed in claim 11, wherein said char and said inert particulate material are exposed to air, causing the char to combust.
13. A process as claimed in claim 12, wherein said reheated inert particulate material flows back into said pyrolytic reactor tube.
14. A process as claimed in any of claims 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12 or 13, wherein upon exiting said pyrolytic reactor tube through said second outlet means, said gaseous material is first cooled and condensed in a primary condenser, and then cooled and condensed in a venturi scrubber.
15. A process as claimed in claim 14, wherein any uncondensed gaseous product flowing from the venturi condenser is filtered through a demister and a filter.
16. A process as claimed in any of claims 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14 or 15, wherein said pyrolytic liquid and gas may be used as a fuel source or as a source of chemical feedstocks.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA002351892A CA2351892C (en) | 2001-06-29 | 2001-06-29 | Process for the conversion of carbonaceous feedstock into liquid, char and gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA002351892A CA2351892C (en) | 2001-06-29 | 2001-06-29 | Process for the conversion of carbonaceous feedstock into liquid, char and gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2351892A1 CA2351892A1 (en) | 2002-12-29 |
| CA2351892C true CA2351892C (en) | 2008-08-26 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002351892A Expired - Lifetime CA2351892C (en) | 2001-06-29 | 2001-06-29 | Process for the conversion of carbonaceous feedstock into liquid, char and gas |
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| CA (1) | CA2351892C (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102005037917A1 (en) | 2005-08-11 | 2007-02-15 | Forschungszentrum Karlsruhe Gmbh | Process for the rapid pyrolysis of lignocellulose |
| SM200700014B (en) * | 2007-04-13 | 2009-11-06 | Antonio Polato | Apparatus for the pyrolysis of organic material, as well as plant and method of treatment of wastewater containing organic material using this apparatus |
| GB2458690B (en) * | 2008-03-28 | 2012-10-03 | Dyfodol Energy Ltd | Treatment of waste plastics material |
| IT1406771B1 (en) | 2010-12-23 | 2014-03-07 | Sea Marconi Technologies Di Vander Tumiatti S A S | MODULAR PLANT FOR THE CONDUCT OF CONVERSION PROCEDURES OF CARBONOUS MATRICES |
| US10513660B2 (en) | 2013-07-19 | 2019-12-24 | ABRI-Tech Inc. | Compact fast pyrolysis system for conversion of carbonaceous materials to liquid, solid and gas |
| US10611966B2 (en) * | 2017-06-21 | 2020-04-07 | Duke Technologies, Llc | Pyrolysis reactor system and method |
| CN108865280B (en) * | 2018-07-17 | 2020-12-08 | 宣城市华科陶粒有限公司 | Crop straw gasification furnace |
| CN112251251A (en) * | 2020-09-29 | 2021-01-22 | 无锡金球机械有限公司 | Industrial continuous classified cracking system and process for mixed waste plastics |
| CN115161050A (en) * | 2022-08-11 | 2022-10-11 | 周文今 | Biomass thermal cracking reaction system and method |
-
2001
- 2001-06-29 CA CA002351892A patent/CA2351892C/en not_active Expired - Lifetime
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| Publication number | Publication date |
|---|---|
| CA2351892A1 (en) | 2002-12-29 |
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