WO2011019901A1 - Installation pour la pyrolyse éclair ou rapide de matières carbonées - Google Patents

Installation pour la pyrolyse éclair ou rapide de matières carbonées Download PDF

Info

Publication number
WO2011019901A1
WO2011019901A1 PCT/US2010/045303 US2010045303W WO2011019901A1 WO 2011019901 A1 WO2011019901 A1 WO 2011019901A1 US 2010045303 W US2010045303 W US 2010045303W WO 2011019901 A1 WO2011019901 A1 WO 2011019901A1
Authority
WO
WIPO (PCT)
Prior art keywords
engine
plant
heat
generator
reactor chamber
Prior art date
Application number
PCT/US2010/045303
Other languages
English (en)
Inventor
Phillip C. Badger
Joshua H. Mcgill
Original Assignee
Badger Phillip C
Mcgill Joshua H
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Badger Phillip C, Mcgill Joshua H filed Critical Badger Phillip C
Publication of WO2011019901A1 publication Critical patent/WO2011019901A1/fr

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
    • 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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
    • C10C5/00—Production of pyroligneous acid distillation of wood, dry distillation of organic waste
    • 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

Definitions

  • the invention relates to a fast pyrolysis plant.
  • a pyrolysis system including a plant for use in the processing of bio-fuels including a base frame having a first end and a second end, as well as a first lateral side and a second lateral side.
  • the plant includes an inlet shaped and dimensioned for the input of carbonaceous feedstock mounted to the base frame adjacent to the first end.
  • a reactor chamber is mounted to the base frame and coupled to the inlet by a feed mechanism which directs
  • a condenser system is positioned and supported along the first lateral side of the base frame by a vertical supporting framework.
  • a char separation and recovery system is mounted upon the base frame and coupled to the reactor chamber by a conveying mechanism for transporting char and heat carrier from the reactor chamber to the char separation and recovery system.
  • the char separation and recovery system is positioned so that its long axis is parallel to the long axis of the base frame.
  • a heat exchanger circulates the heat carrier from the char separation and recovery system back to the reactor chamber.
  • crankcase oil cooler is linked to the engine-generator and heat recovered from the engine oil cooler for use by the plant or other application.
  • It is another object of the present invention to provide a pyrolysis system for use in the processing of bio-fuels including a base frame having a first end and a second end, as well as a first lateral side and a second lateral side.
  • the plant includes an inlet shaped and dimensioned for the input of carbonaceous feedstock mounted to the base frame adjacent to the first end with a dryer in communication with the input.
  • a reactor chamber is mounted to the base frame and coupled to the inlet by a feed mechanism which directs carbonaceous feedstock from the inlet to the reactor chamber.
  • a condenser system is positioned and supported along the first lateral side of the base frame by a vertical supporting framework.
  • a char separation and recovery system is mounted upon the base frame and coupled to the reactor chamber by a conveying mechanism for transporting char and heat carrier from the reactor chamber to the char separation and recovery system.
  • a heat exchanger circulates the heat carrier from the char separation and recovery system back to the reactor chamber.
  • An engine-generator is linked to a furnace, wherein the engine-generator supplies heat to the furnace and the furnace boosts in temperature the heat generated by the engine- generator for use by the plant.
  • Figure 1 is a perspective view of the present plant.
  • Figures 2, 3 and 4 are schematics showing the relationship between the reactor chamber and the char separation and recovery system.
  • Figure 5 is a perspective view of the present plant within a shipping container and with associated components attached thereto.
  • Figure 6 is a flow chart showing operation of the present fast pyrolysis system.
  • Figure 7 is a perspective view of an alternate embodiment of the present plant within a shipping container and with associated components attached thereto.
  • FIGS 8 and 9 are flow charts showing operation of the alternate system shown with reference to Figure 7.
  • a fast pyrolysis system 1 employing a plant 10 for use in the processing of bio-fuels.
  • the plant 10 converts carbonaceous feedstock into energy, such as, gaseous, liquid and char products in accordance with the present invention.
  • the carbonaceous feedstock may, for example, be biomass.
  • the feedstock In order for the present plant 10 to work properly, the feedstock must be ground to a fine consistency and dried.
  • the plant 10 generally implements the same components and concepts for the processing of bio-fuels as disclosed in commonly owned U.S. Patent Application Serial No. 11/480,914, filed July 6, 2006, which was been published as U.S. Patent Application Publication No. 2008/0006519 on January 10, 2008, entitled "METHOD AND SYSTEM FOR ACCOMPLISHING FLASH OR FAST PYROLYSIS WITH CARBONACEOUS MATERIALS", which is incorporated herein by reference.
  • char is meant to refer to carbon-rich matter that has been partially, but incompletely, devolatized when subjected to heat in a controlled manner for a predetermined period of time.
  • the application of heat to the feedstock in an oxygen depleted atmosphere results in the removal of some hydrogen, oxygen and carbon from the feedstock, leaving a char material primarily composed of carbon.
  • the fast pyrolysis process as implemented through the use of the present plant 10 employs a dryer 80 into which carbonaceous feedstock, such as biomass, for example, wood at 30% moisture content and having approximately 12.6 MBtu of available energy, is placed.
  • carbonaceous feedstock such as biomass, for example, wood at 30% moisture content and having approximately 12.6 MBtu of available energy
  • the feedstock must be ground to a fine consistency and dried.
  • the equipment used in grinding and drying of the feedstock is readily available, and various known devices may be employed for this purpose.
  • the dried feedstock is forwarded to the reactor chamber 14 via a conveyor 15 and inlet 26 with the emissions from the dryer 80 forwarded to a cyclone and/or bag house 82 (or other suitable device which removes pollutants from the emission stream).
  • a cyclone and/or bag house 82 or other suitable device which removes pollutants from the emission stream.
  • the cyclone and/or bag house 82 may be replaced or supplemented with a wet scrubber or other suitable device known to those skilled in the art for the control of emissions.
  • the dried biomass for example, the dried wood
  • the dried biomass is transferred to the reactor chamber 14 which operates at approximately 662°F (350° C) to approximately 1,040 0 F (560° C). While drying of the feedstock is disclosed in accordance with a preferred embodiment of the present invention, those skilled in the art will appreciate that drying is not always necessary as some feedstock arrives dry enough for processing and the drying step may be skipped.
  • Gas and vapor from the reactor chamber 14 is passed through a condenser system 38 as discussed below in greater detail and the vapor is condensed to recover the liquid product.
  • This liquid product is known by several names including bio-oil, pyrolysis oil, wood distillate, and other names, and is composed of water and numerous chemicals.
  • Useful gas, for example, syngas is recovered as it exits the condenser system 38.
  • the bio-oil is collected for later use and the syngas is forwarded to a furnace 41, where it is combusted to provide at least part of the energy for the fast pyrolysis process.
  • syngas could be used to fuel an engine to generate heat and electricity for the system or used in other ways, such as feedstock for chemical production or for applications separate from the fast pyrolysis plant.
  • syngas or synthesis gas
  • the bio-oil may be used as an energy source or a source of chemicals, or for other applications, in much the same manner as petroleum products.
  • the char (and its inherent ash) and heat carrier 12 are transferred from the pyrolytic reactor chamber 14 to the char separation and recovery system 44.
  • the char separation and recovery system 44 separates the heat carrier (HC) 12, which is transferred to a heat exchanger 68 to be reheated and recirculated to the reactor chamber 14, and the char, which is collected and, to the extent necessary needed for process energy, burned in the furnace 41. Any char not needed for process energy becomes a coproduct.
  • the hot heat carrier 12, when mixed with the feedstock in the reactor chamber 14, provides the thermal energy for pyrolysis to occur in the reactor chamber 14 without the introduction of oxygen into the reactor chamber 14.
  • the method is achieved by drying carbonaceous feedstock (if necessary), processing the dried carbonaceous feedstock with heat from the heat carrier 12 in a reactor chamber 14, separating char produced as a result of processing of feedstock within the reactor chamber 14 from heat carrier 12, separating and recovering liquid product and non-condensable gases from gas and vapor emitted by the reactor chamber 14, and burning the non-condensable gases and char as needed to provide energy for operation of the method.
  • the plant 10 may include a base frame 16 upon which the operating components of the processing plant 10 are mounted. If mounted within a modular container 84, the container 84 itself can serve as the plant frame.
  • the processing plant 10 is specifically designed for positioning within standard size shipping containers, although small portions may extend beyond the walls of the container 84 as shown with regard to the condenser system 38 shown in Figure 3.
  • the plant 10 should fit within an 9.5 foot (290 cm) (width) by 8 foot (244 cm) (height) by 48 foot (1463 cm) (length) container (occupying approximately 3,648 cubic feet (104 cubic meters) of space)) used in overseas shipping or similar module suitable for over-the-road transportation as governed by the United States Department of Transportation, Rules and Regulations, Part 658, Size and Weight, Route Designations - Length, Width and Weight
  • the base frame 16 is typically constructed of metal fastened (for example, welded) together in a rectangular configuration.
  • the base frame 16 includes a first end 18 and a second end 20, as well as a first lateral side 22 and a second lateral side 24.
  • An inlet 26 is mounted to the base frame 16 adjacent the first end 18.
  • the inlet 26 is shaped and dimensioned for the input of carbonaceous feedstock. It is
  • the inlet 26 may be connected to the dryer 80 via a conveyor 15 as shown in Figure 5.
  • a conveyor 15 as shown in Figure 5.
  • the equipment used in grinding and drying of the feedstock is readily available, and various known devices may be employed for this purpose.
  • the carbonaceous feedstock is directed from the inlet 26 to the reactor chamber 14 by virtue of a feed mechanism 30.
  • the feed mechanism 30 includes a rotating feed auger.
  • the rotating feed auger is a conventional centerless auger (i.e., shaftless auger), although an auger with a center shaft may be used, in a tube or one or more side-by-side augers which may or may not be in a common trough as disclosed in commonly owned U.S. Patent Application Serial No. 11/480,914, filed July 6, 2006, which was been published as U.S. Patent Application Publication No. 2008/0006519 on January 10, 2008, entitled "METHOD AND SYSTEM FOR ACCOMPLISHING FLASH OR FAST PYROLYSIS WITH CARBONACEOUS MATERIALS", which is incorporated herein by reference.
  • the feed mechanism 30 is composed of a rotating feed auger with a motorized star wheel airlock (not shown) positioned above the rotating feed auger and at the auger end opposite the reactor chamber 14.
  • the motorized star wheel airlock drops material through an air gap into the rotating feed auger to improve the air seal and reduce the chances for burn back.
  • the airlock is more important for granular, or other, materials that do not naturally compact when conveyed by an auger.
  • the reactor chamber 14 is mounted at the first end 18 of the base frame 16 adjacent the inlet 26.
  • a dryer 80 is used, the emissions from the dryer 80 are forwarded to a cyclone and/or bag house 82 or other emission control devices, if emission control devices are necessary.
  • the cyclone and/or bag house may be replaced or supplemented with a wet scrubber or other suitable device known to those skilled in the art for the control of emissions. While drying of the feedstock is disclosed in accordance with a preferred embodiment of the present invention, those skilled in the art will appreciate that drying is not always necessary as some feedstock arrives dry enough for processing and the drying step may be skipped.
  • the dry biomass for example, the dried wood, is transferred to the reactor chamber 14 which operates at approximately 662 0 F (350° C) to approximately
  • the carbonaceous feedstock enters the pyrolytic reactor chamber 14, which houses a rotating auger or some other mixing device (not shown), and wherein the feed stock is mixed with a heat carrier 12.
  • the carbonaceous feedstock is formed into plugs as the feedstock is conveyed by the feed mechanism 30.
  • the formation of plugs excludes air from the reactor chamber 14.
  • the heat carrier 12 is hot steel shot, although a variety of heat carriers may be utilized without departing from the spirit of the present invention.
  • the gas and vapor generated by the reactor chamber 14 are passed through a condenser system 38.
  • the condenser system 38 is positioned and supported along the first lateral side 22 of the base frame 16 by a vertical supporting framework 39 and is also positioned adjacent the reactor chamber 14 for easy transmission of the gas and vapor products thereto.
  • the liquid product produced in accordance with the present plant 10 is known by several names including bio-oil, pyrolysis oil, wood distillate and other names, and is composed of water and numerous chemicals.
  • Useful gas, for example, syngas is recovered as it exits the condenser system 38.
  • the bio-oil is collected for later use and the syngas is forwarded to a furnace 41 (that is, the char/syngas/bio-oil burner that may be connected to the plant 10 for receipt of the bio-oil) where it is combusted to provide at least part of the energy for the plant 10.
  • the syngas could be used to fuel an engine (which can be in various forms) to generate heat and electricity for the plant 10.
  • syngas (or synthesis gas) is the non-condensable gas portion of the gas and vapor stream from the reactor chamber 14 and has energy value.
  • the bio-oil may be used as an energy source or a source of chemicals, or for other applications, in much the same manner as petroleum products.
  • the gas and vapor depart the pyrolytic reactor chamber 14 via a tube 32 and are directed to the condenser system 38 or, alternatively, the gas and vapor— comprising a syngas— may be used for energy directly without a condenser system 38.
  • Condensed liquids for example, bio-oil, are collected by virtue of tanks and then transferred with pumps.
  • the gas and vapor Prior to entering the condenser system 38, the gas and vapor are cleansed by passing it through a char trap 70 and a tar trap 72, as well as other suitable cleansing devices (also positioned and supported along the first lateral side 22 of the base frame 16 by the vertical supporting framework 39).
  • the cleansed vapor and gaseous material are then directed to a condenser system 38 and the condensed liquids (for example, including bio-oil) from the condenser system 38 are transferred to storage tanks 49 by gravity or by virtue of one or more liquid transfer pumps.
  • the condenser system 38 is in fluid communication with a fluid air heat exchanger 40 mounted at the second end 20 of the base frame 16.
  • the uncondensed gases which can contain considerable energy value (for example in the form of syngas), are also recovered and used for energy by directing them to a char/syngas/bio-oil burner, that is, a furnace, 41 or for applications independent of the pyrolysis process.
  • the uncondensed gases may be used for energy by using the uncondensed gases to fuel an engine (for example, reciprocating internal combustion engine, combustion turbine, or Stirling engine) to provide mechanical and/or electrical power and heat for the process.
  • an engine for example, reciprocating internal combustion engine, combustion turbine, or Stirling engine
  • there can be enough energy in the uncondensed gas to supply all the electrical and/or heat requirements of the present plant 10.
  • the use of the uncondensed gas, bio-oil, and char can thus minimize or eliminate the need for external energy sources which reduces operating expense and may allow the units to be operated in remote areas (for example, military camps and/or logging camps).
  • condensation columns 42 may be employed.
  • condensation columns 42 may be employed.
  • fractional condensation column (s) 42 include a series of plates which are connected directly to the reactor chamber(s) 14 (typically above the reactor chamber 14 to take advantage of the tendency of the warm, low-density vapor to rise) to create an integral unit so that the gas and vapor generated by the process in the reactor chamber 14 are continuously and immediately passed through the condensation columns 42.
  • the fractional condensers could take other forms and be located separately from the reactor chamber and connected to the reactor chamber by ducting or piping.
  • the char, ash and heat carrier 12 are transferred from the pyrolytic reactor chamber 14 to the char separation and recovery system 44 mounted at an opposite end of the base frame from the reactor chamber 14.
  • the preferred embodiment of the char separation and recovery system 44 includes a trommel screen inclined at an angle from zero to 15 degrees.
  • the char separation and recovery system 44 is positioned so that its long axis 44a is parallel to the long axis 16a of the shipping container 84 and base frame 16, and the vertical plane in which the axis 36a of augers 34 and 46 lies is parallel to the vertical plane in which the long axis 16a of the base frame 16 and the shipping container 84 lie.
  • the char, ash and the heat carrier 12 exit the pyrolytic reactor chamber 14 and are transported via an auger (or other conveying mechanism) 46 to the separation and recovery system 44 in which the heat carrier 12 is recovered for further use and separated from the char.
  • the char which contains the feedstock ash
  • the char storage hopper not shown
  • an outlet 48 of the separation and recovery system 44 or some other conveying mechanism.
  • char product is removed and, as needed for process heat, a portion of the char is transported to the char/syngas/bio-oil burner (or furnace) 41.
  • char is separated out from the heat carrier 12 by the separation and recovery system 44, and conveyed via the outlet 48 to a lock hopper (not shown) for storage.
  • the separation and recovery system 44 employs mechanisms as disclosed in commonly owned U.S. Patent Application Serial No. 11/480,914, filed July 6, 2006, which was been published as U.S. Patent Application Publication No. 2008/0006519 on January 10, 2008, entitled "METHOD AND SYSTEM FOR ACCOMPLISHING FLASH OR FAST
  • the separation and recovery system 44 implements a trommel screen 45, the long axis 45a of which is aligned with the long axis 44a of the separation and recovery system 44 such that it is oriented parallel to the long axis 16a of the shipping container 84 and base frame 16.
  • the char separation and recovery system 44 separates the heat carrier 12, which is transferred to a heat exchanger 68 to be reheated as it is recirculated to the reactor chamber 14, and the char, which is collected and, to the extent necessary for process heat, burned in the furnace 41.
  • the heat carrier 12 is circulated back to the reactor chamber 14 via a heat exchanger 68 constructed as disclosed in commonly owned U.S. Patent Application Serial No. 11/480,914, filed July 6, 2006, which was been published as U.S. Patent Application Publication No. 2008/0006519 on January 10, 2008, entitled "METHOD AND SYSTEM FOR ACCOMPLISHING FLASH OR FAST
  • the heat exchanger 68 includes an auger mechanism 34 for conveying the heat carrier 12 and a heat exchanger chamber 36 surrounding the auger mechanism 34 for the transfer of heat thereto for application to the heat carrier 12 as it is moved by the auger mechanism 34.
  • the heat for the heat exchanger chamber 36 is supplied by the furnace 41 via a tube 50 connected between the heat exchanger 68 and the furnace 41. Any char not needed for process heat becomes a coproduct.
  • the present invention provides a
  • the present invention minimizes the energy requirements of an innovative fast pyrolysis process through energy recovery and, in combination with self-use of a portion of its energy products, can under some conditions, attain plant energy self-sufficiency.
  • the fast reaction times associated with fast pyrolysis means that large amounts of carbonaceous materials can be processed in a relatively small footprint as discussed and disclosed above with regard to the present processing plant 110 that is designed for positioning within standard size shipping containers 184 or to provide a readily transportable modular configuration for ease of distribution and installation.
  • This feature coupled with the simplicity of the fast pyrolysis technology discussed above and disclosed in commonly owned U.S. Patent Application Serial No. 11/480,914, filed July 6, 2006, which was been published as U.S. Patent Application Publication No.
  • thermochemical processes use heat in the absence of oxygen (typically in the range of 660 0 F to 1020 0 F (350 0 C to 550 0 C), depending on feedstock characteristics and other factors) to breakdown carbonaceous materials into gases (roughly 75% yield) and char (roughly 25% yield).
  • the condensable gases (roughly 80% of the gases) are recovered as liquids after condensation leaving the non-condensable gases, which typically have an aggregated energy value in the range of 250 to 300 Btu/ft3.
  • the char product can have energy values in the range of 12,000 Btu/lb.
  • the method of heating the contents of the fast pyrolysis reactor chamber 114 may vary widely but all fast pyrolysis processes require that the carbonaceous materials be heated to the desired process temperature in roughly 1 second. Heat is required for the fast pyrolysis reactions and, depending on feedstock input requirements and quality, for drying the feedstock. Electrical energy is required for process materials handling and control and, depending on design, other purposes.
  • the present invention allows one to complete the fast pyrolysis process in an energy self-sufficient (to the extent possible) manner, including facilitating the operation of transportable plants 110, especially the operation of plants 110 in remote areas away from traditional infrastructure. Additionally, syngas is produced continuously as the fast pyrolysis process is operating and this gas is not readily compressible or storable. While traditional disposal of this gas by flaring complicates environmental permitting and wastes valuable energy, the present invention employs this syngas in an efficient and effective manner.
  • the present invention integrates an engine-generator 190 into the fast pyrolysis process with heat recovery and electrical energy generation from the engine-generator 190 for providing both electrical and thermal energy required for operation and control of the present fast pyrolysis plant 110.
  • this engine-generator 190 is fueled with syngas or the liquid fuel product generated as a result of operation of the present process, or the fuels together. If necessary or desired, it is contemplated this engine- generator 190 could also use conventional fuels (e.g., diesel fuel).
  • this engine-generator 190 can be an external combustion engine or internal combustion engine (preferred embodiment) including reciprocating engines and combustion turbines and no limitation is placed on the type of heat engine, although some engines are better suited than others for this application. Electrical energy could also be generated through the use of thermopiles or other means and thermal energy recovered from these methods. Since electricity is the most expensive form of energy required in the fast pyrolysis process, sound engineering design requires that the engine-generator 190 be sized to meet the process electrical requirements (although alternative design methods could be used). The method of design dictates the amount of waste heat available. Additionally, the type of prime mover (engine) dictates the form and quality of waste heat available.
  • Heat is available from the engine-generator 190 in the form of hot air exhaust, hot radiator fluid or air from the radiator, and hot air from the crankcase engine oil cooler, if so equipped.
  • a radiator 192 and crankcase oil cooler 194 are linked to the engine-generator 190 (in accordance with a preferred embodiment, the radiator and oil cooler are integrated with the engine generator 190) for extracting heat, which is subsequently used in supplying heat to the dryer 180 or other applications via supply lines 196, 198.
  • heat can be recovered from the radiator in a liquid heat transfer medium such as a water/glycol solution (typical temperature 180 0 F (82 0 C) to 200 0 F (93 0 C)) or as hot air from the radiator (typical temperatures 8O 0 F (26°C) to 130 0 F (54°C), depending on ambient conditions and other factors.
  • a liquid heat transfer medium such as a water/glycol solution (typical temperature 180 0 F (82 0 C) to 200 0 F (93 0 C)) or as hot air from the radiator (typical temperatures 8O 0 F (26°C) to 130 0 F (54°C), depending on ambient conditions and other factors.
  • heat engine-generator uses an oil cooler
  • heat may be recovered from the hot oil with typical oil temperatures in the range of 25O 0 F (121 0 C).
  • Typical exhaust temperatures from a combustion turbine with a recuperator are 500 0 F (260 0 C) and without a recuperator, 900 0 F (482°C).
  • temperatures required for process heat transfer may be in the range of 1200 0 F (649 0 C) to 1600 0 F (871°C), more or less, depending on desired process operating temperatures, mode of heat transfer to the contents of the reactor, and other factors.
  • temperatures provided by heat recovery from the engine-generator 190 alone are not high enough for indirectly heating fast pyrolysis reactors (for example, transferring heat to the heat carrier for the fast pyrolysis reaction) and, additionally, the heat recovered from the engine-generator 190 may not provide enough energy for both the fast pyrolysis reactor chamber 114 and associated process dryer 180 operations.
  • the present invention employs the heat of the exhaust 199 from the engine-generator 190 by connecting it to the furnace 141 via tube 200. After being directed to the furnace 141, the heat of the exhaust 199 is passed into the heat exchanger 168 (connecting the char separation and recovery system 144 with the reactor chamber 114) with the heat generated by the furnace 141 to boost the exhaust temperature to that desired for providing heat to the fast pyrolysis reaction and, if necessary, the additional energy required for the process operations or other purposes.
  • the heat for this heat exchanger 168 comes from both the furnace 141 and the engine-generator 190; that is, the furnace 141 boosts in temperature heat generated by the engine-generator 190 and adds energy to the heat (that is, the exhaust 199) generated by the engine-generator 190.
  • the furnace 141 can use syngas, bio-oil, or char from the process as fuels (the preferred embodiment) and may be supplemented if necessary or desired with other fuels. Additionally, this heat could come from a source external to the fast pyrolysis process, such as from a co-located process or heat source.
  • Another element incorporated into this embodiment involves the use of heat recovered from the heat carrier heat exchanger 168. Temperature drops for the heat carrier through the heat carrier heat exchanger can range from 100 0 F (38°C) to 600 0 F (316 0 C), thus considerable thermal energy remains in the heat carrier (or heat transfer medium) after the fast pyrolysis reactor chamber 114 and can be recovered and used for drying the incoming feedstock to increase overall process efficiency by linking the heat carrier heat exchanger 168 with the dryer 180 via tubing 202 (see Figures 8 and 9). Many feedstocks may have initial moisture contents in the range of 50% (wet basis) while good fast pyrolysis efficiencies typically require feedstock moisture contents in the range of 10% or less.
  • Feedstock drying can be accomplished at temperatures as low as 25O 0 F (121 0 C), thus thermal energy in the heat transfer medium from the fast pyrolysis reactor can be recovered and used either directly (the preferred embodiment) or indirectly as a thermal energy source for the dryer. Depending on initial feedstock moisture content and other factors, all of the energy required for drying the feedstock can be provided in this manner.
  • additional thermal energy may also be recovered from the engine radiator 192 or oil cooler 194 and blended into the thermal energy stream from the heat carrier heat exchanger 168 into the dryer 180, or used for other purposes. If the energy requirements of the dryer 180 are greater than the thermal energy recovered from the heat carrier heat exchanger 168, some of the thermal energy generated by the engine-generator 190 and furnace 141 can bypass the heat carrier heat exchanger (via tube 204) and go directly to the dryer 180 or another application. In some situations, air that is cooler, such as ambient air, may need to be added to the air inlet to the dryer to reduce the temperatures of the air from the heat transfer medium from the engine, furnace, or reactor. This description of possible energy flows is not meant to be exclusive and other combinations are possible.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Combustion & Propulsion (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

Un système de pyrolyse rapide emploie une installation destinée à être utilisée dans le traitement de biocarburants. L'installation comprend un châssis de base ayant une première extrémité et une seconde extrémité, ainsi qu'un premier côté latéral et un second côté latéral. L'installation comprend également une entrée de forme et de dimension appropriées pour l'entrée d'une charge d'alimentation carbonée montée sur le châssis de base à proximité de la première extrémité, une chambre de réacteur montée sur le châssis de base et raccordée à l'entrée par un mécanisme d'alimentation qui achemine la charge d'alimentation carbonée de l'entrée vers la chambre du réacteur, un système condenseur placé et supporté le long du premier côté latéral du châssis de base par une structure support verticale, un système de séparation et de récupération de produit de carbonisation monté sur le châssis de base et raccordé à la chambre du réacteur par une vis sans fin pour le transport de produit de carbonisation et de caloporteur de la chambre du réacteur vers le système de séparation et de récupération de produit de carbonisation et un échangeur de chaleur renvoyant le caloporteur du système de séparation et de récupération de produit de carbonisation vers la chambre du réacteur. Le système comprend également un moteur-générateur relié à un four, le moteur-générateur fournissant de la chaleur au four et le four augmentant la température de la chaleur produite par le moteur-générateur destinée à être utilisée par l'installation.
PCT/US2010/045303 2009-08-14 2010-08-12 Installation pour la pyrolyse éclair ou rapide de matières carbonées WO2011019901A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US23410809P 2009-08-14 2009-08-14
US61/234,108 2009-08-14
US12/854,993 US20110035998A1 (en) 2009-08-14 2010-08-12 Plant for the flash or fast pyrolysis of carbonaceous materials
US12/854,993 2010-08-12

Publications (1)

Publication Number Publication Date
WO2011019901A1 true WO2011019901A1 (fr) 2011-02-17

Family

ID=43586482

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2010/045303 WO2011019901A1 (fr) 2009-08-14 2010-08-12 Installation pour la pyrolyse éclair ou rapide de matières carbonées

Country Status (2)

Country Link
US (1) US20110035998A1 (fr)
WO (1) WO2011019901A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2503065A (en) * 2013-02-20 2013-12-18 Recycling Technologies Ltd Process and apparatus for treating waste comprising mixed plastic waste
EP2978821B1 (fr) * 2013-03-28 2020-11-11 Carbon Gold Limited Procédé de production de biochar

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FI124016B (fi) * 2009-10-26 2014-01-31 Vapo Oy Menetelmä biomassakuivattimessa käytetyn kuivatusilman lämmittämiseksi välipiirinesteen avulla sekä vesi-glykoliseoksen tai sitä vastaavan jäätymättömän välipiirinesteen käyttö biomassakuivattimessa käytetyn kuivatusilman lämmittämiseksi
CA2704186A1 (fr) 2010-05-18 2011-11-18 Lucie B. Wheeler Reacteur de craquage thermique pour melanges, procedes correspondants et leurs utilisations
US20120228112A1 (en) * 2011-03-08 2012-09-13 Mississippi State University Thermal transfer mechanisms for an auger pyrolysis reactor
WO2013151571A1 (fr) * 2012-04-02 2013-10-10 De Lima Jose Railton Souza Système et appareil pour la production d'électricité à partir de masse végétale et animale
CA2783608A1 (fr) 2012-07-23 2014-01-23 Lucie Wheeler Procede environnemental visant a transformer une matiere d'alimentation contaminee ou decontaminee en des produits utiles, utilisations du procede, produits ainsi obtenus et utilisations de ceux-ci et fabrication de l'installation correspondante
CA2938502A1 (fr) * 2013-02-06 2014-08-06 Envirollea Inc. Station mobile de traitement thermique d'un courant d'alimentation contamine ou non, procedes associes et utilisations de produits associees
CA2899362C (fr) 2013-02-06 2017-10-17 Envirollea Inc. Procede thermique visant a transformer des matieres premieres contaminees ou decontaminees en produits huileux utiles
CA2973210A1 (fr) * 2017-07-13 2019-01-13 Louis Bertrand Procede de production de combustible liquide a partir de rejets d'hydrocarbure ou de matiere organique, systeme de gestion associe
CA3056050C (fr) 2019-02-04 2020-04-28 Envirollea Inc. Huiles de flottaison, procedes et utilisations associees
WO2024081951A1 (fr) * 2022-10-14 2024-04-18 Myno Carbon Corp. Systèmes sensibles au contexte et procédés de fonctionnement d'une installation d'élimination de carbone

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070220810A1 (en) * 2006-03-24 2007-09-27 Leveson Philip D Method for improving gasification efficiency through the use of waste heat
US20080006519A1 (en) * 2006-07-06 2008-01-10 Badger Phillip C Method and system for accomplishing flash or fast pyrolysis with carbonaceous materials
US20090013601A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Modular and distributed methods and systems to convert biomass to syngas

Family Cites Families (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4153514A (en) * 1975-02-27 1979-05-08 Occidental Petroleum Corporation Pyrolysis process for solid wastes
US4085030A (en) * 1976-06-25 1978-04-18 Occidental Petroleum Corporation Pyrolysis of carbonaceous materials with solvent quench recovery
US4284616A (en) * 1978-02-15 1981-08-18 Intenco, Inc. Process for recovering carbon black and hydrocarbons from used tires
US4246093A (en) * 1979-07-26 1981-01-20 Atlantic Richfield Company Handling of solids-laden hydrocarbonaceous bottoms in a retort using solid heat-carriers
US4261795A (en) * 1979-11-16 1981-04-14 Reilly Bertram B Apparatus for solid waste pyrolysis
US4478039A (en) * 1980-12-29 1984-10-23 United Technologies Corporation Utilization of coal in a combined cycle powerplant
US4994297A (en) * 1987-11-12 1991-02-19 Ensyn Engineering Associates, Inc. Method of using fast pyrolysis liquids as liquid smoke
US5270067A (en) * 1987-11-12 1993-12-14 Red Arrow Products Company Inc. Impregnated casing and method of making the same
US5091499A (en) * 1988-03-17 1992-02-25 Midwest Research Institute Process for preparing phenolic formaldehyde resole resin products derived from fractionated fast-pyrolysis oils
US5292541A (en) * 1989-05-26 1994-03-08 Red Arrow Products Company Inc. Browning materials derived from the pyrolysis of sugars and starches
US5397582A (en) * 1989-05-26 1995-03-14 Red Arrow Products Company Inc. Flavoring and browning materials by pyrolysis of sugars and starches
US5961786A (en) * 1990-01-31 1999-10-05 Ensyn Technologies Inc. Apparatus for a circulating bed transport fast pyrolysis reactor system
US5792340A (en) * 1990-01-31 1998-08-11 Ensyn Technologies, Inc. Method and apparatus for a circulating bed transport fast pyrolysis reactor system
US5252188A (en) * 1990-03-26 1993-10-12 Red Arrow Products Company, Inc. Process for producing hydroxyacetaldehyde
US5852029A (en) * 1990-04-10 1998-12-22 Israel Institute For Biological Research Aza spiro compounds acting on the cholinergic system with muscarinic agonist activity
CA2099318A1 (fr) * 1993-06-28 1994-12-29 Peter Fransham Traitement thermolytique des piquets enduits de pentachlorophenol
US5458803B1 (en) * 1993-09-30 1999-08-03 Dynamotive Corp Acid emission reduction
US5817282A (en) * 1996-03-28 1998-10-06 Dynamotive Technologies Corporation Reduction of nitrogen oxides
US6902711B1 (en) * 1996-04-23 2005-06-07 Ebara Corporation Apparatus for treating wastes by gasification
US5728271A (en) * 1996-05-20 1998-03-17 Rti Resource Transforms International Ltd. Energy efficient liquefaction of biomaterials by thermolysis
US6326461B1 (en) * 1998-01-30 2001-12-04 Ensyn Group, Inc. Natural resin formulations
US6485841B1 (en) * 1998-10-30 2002-11-26 Ensyn Technologies, Inc. Bio-oil preservatives
US6143856A (en) * 1999-01-29 2000-11-07 Pyrovac Technologies Inc. Process for the production of phenolic-rich pyrolysis oils for use in making phenol-formaldehyde resole resins
AUPQ744500A0 (en) * 2000-05-11 2000-06-01 Scott, Franklin Biomass burner
EP1217318A1 (fr) * 2000-12-19 2002-06-26 Sea Marconi Technologies Di Wander Tumiatti S.A.S. Installation pour le traitement thermique d'un matériau et procédé pour son fonctionnement
US6979426B2 (en) * 2002-03-15 2005-12-27 Biodiesel Industries Biodiesel production unit
US7004999B2 (en) * 2003-08-18 2006-02-28 Dynamotive Energy Systems Corporation Apparatus for separating fouling contaminants from non-condensable gases at the end of a pyrolysis/thermolysis of biomass process
US20080006520A1 (en) * 2006-07-06 2008-01-10 Badger Phillip C Method and system for accomplishing flash or fast pyrolysis with carbonaceous materials

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070220810A1 (en) * 2006-03-24 2007-09-27 Leveson Philip D Method for improving gasification efficiency through the use of waste heat
US20080006519A1 (en) * 2006-07-06 2008-01-10 Badger Phillip C Method and system for accomplishing flash or fast pyrolysis with carbonaceous materials
US20090013601A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Modular and distributed methods and systems to convert biomass to syngas

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2503065A (en) * 2013-02-20 2013-12-18 Recycling Technologies Ltd Process and apparatus for treating waste comprising mixed plastic waste
GB2503065B (en) * 2013-02-20 2014-11-05 Recycling Technologies Ltd Process and apparatus for treating waste comprising mixed plastic waste
US10093860B2 (en) 2013-02-20 2018-10-09 Recycling Technologies Ltd Process and apparatus for treating waste comprising mixed plastic waste
US10717934B2 (en) 2013-02-20 2020-07-21 Recycling Technologies Ltd. Apparatus for treating waste comprising mixed plastic waste
US10760003B2 (en) 2013-02-20 2020-09-01 Recycling Technologies Ltd Process and apparatus for treating waste comprising mixed plastic waste
EP2978821B1 (fr) * 2013-03-28 2020-11-11 Carbon Gold Limited Procédé de production de biochar

Also Published As

Publication number Publication date
US20110035998A1 (en) 2011-02-17

Similar Documents

Publication Publication Date Title
US20110035998A1 (en) Plant for the flash or fast pyrolysis of carbonaceous materials
CA2772537C (fr) Systeme et procede pour une gazeification descendante
DK2597137T3 (en) Method and apparatus for biomass pyrolysis gasification via two interconnected furnaces
KR20110137345A (ko) 바이오매스의 재활용 방법 및 시스템 그리고 블록 열 발전 설비
KR100993908B1 (ko) 가연성 폐기물의 에너지 연료화 방법 및 가연성 폐기물의 가스화 장치
JP7050043B2 (ja) 廃棄物処理システム
US20100275823A1 (en) Special Pyrogen Waste treatment and electrical generation combination of systems
CN111989169B (zh) 废弃物处理系统以及废弃物处理方法
KR101632147B1 (ko) 바이오매스 발전설비
KR101632146B1 (ko) 바이오매스 가스화 장치
US20150083571A1 (en) System and Method Using a Horizontal Sublimation Chamber for Production of Fuel From a Carbon-Containing Feedstock
US10280377B1 (en) Pyrolysis and steam cracking system
US8206471B1 (en) Systems, apparatus and methods for optimizing the production of energy products from biomass, such as sawmill waste
JP7101160B2 (ja) 廃棄物処理システム
JP2018017494A (ja) リサイクル資源製造装置
JP7101159B2 (ja) 廃棄物処理システム
US20190072275A1 (en) Solid and Black Waste Mitigation System and Process
KR102209991B1 (ko) 바이오매스 급속열분해용 유동층 반응기를 통하여 제조된 바이오원유의 합성가스 시스템
RU2737833C1 (ru) Способ автономной электрогенерации и устройство - малая твердотопливная электростанция для его осуществления
JP7101158B2 (ja) 廃棄物処理システム
Bhattacharya et al. An update technology for integrated biomass gasification combined cycle power plant
RU2631455C1 (ru) Способ получения электроэнергии из некондиционной (влажной) топливной биомассы и устройство для его осуществления
WO2023111376A1 (fr) Procédé de valorisation de matériau de rebut
EA042053B1 (ru) Способ и когенерационная установка для генерации электроэнергии с использованием органического цикла ренкина
FR3018559A1 (fr) Installation de production d'energie a partir de la biomasse et de l'energie solaire

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 10808751

Country of ref document: EP

Kind code of ref document: A1

122 Ep: pct application non-entry in european phase

Ref document number: 10808751

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE