EP2729749A1 - Système et procédé pour la conversion de matière organique en produit torréfié - Google Patents

Système et procédé pour la conversion de matière organique en produit torréfié

Info

Publication number
EP2729749A1
EP2729749A1 EP12807598.3A EP12807598A EP2729749A1 EP 2729749 A1 EP2729749 A1 EP 2729749A1 EP 12807598 A EP12807598 A EP 12807598A EP 2729749 A1 EP2729749 A1 EP 2729749A1
Authority
EP
European Patent Office
Prior art keywords
kiln
feedstock
test
product
burner assembly
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.)
Withdrawn
Application number
EP12807598.3A
Other languages
German (de)
English (en)
Other versions
EP2729749A4 (fr
Inventor
Anjali VARMA
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
TORREFUELS Inc
Original Assignee
TORREFUELS Inc
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 TORREFUELS Inc filed Critical TORREFUELS Inc
Publication of EP2729749A1 publication Critical patent/EP2729749A1/fr
Publication of EP2729749A4 publication Critical patent/EP2729749A4/fr
Withdrawn legal-status Critical Current

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
    • 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
    • C10B49/02—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/08—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
    • C10B49/12—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form by mixing tangentially, e.g. in vortex chambers
    • 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
    • C10B1/00—Retorts
    • C10B1/10—Rotary retorts
    • 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
    • C10B49/02—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • 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
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • C10L9/083—Torrefaction
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F23G5/0276—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage using direct heating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • F23G5/16—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion in a separate combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/20—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having rotating or oscillating drums
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F23G5/442—Waste feed arrangements
    • F23G5/444—Waste feed arrangements for solid waste
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F23G5/46—Recuperation of heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/10—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of field or garden waste or biomasses
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/06—Rotary-drum furnaces, i.e. horizontal or slightly inclined adapted for treating the charge in vacuum or special atmosphere
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
    • F27B7/32—Arrangement of devices for charging
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
    • F27B7/33—Arrangement of devices for discharging
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
    • F27B7/34—Arrangements of heating devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/303—Burning pyrogases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2205/00—Waste feed arrangements
    • F23G2205/12—Waste feed arrangements using conveyors
    • F23G2205/121—Screw conveyor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/26—Biowaste
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2900/00—Special features of, or arrangements for incinerators
    • F23G2900/00001—Exhaust gas recirculation
    • 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 present invention pertains to the field of renewable energy and, in particular, to a system and process for conversion of organic matter (such as biomass feedstock) into a torrefied product.
  • Torrefaction is a thermal process used to convert biomass in an oxygen-deficient environment into a high-quality biochar. Torrefaction as a process to generate renewable fuel has long been sought after. The concept that this process can transform biomass into a product that is stored, handled, burned and has properties similar to coal is extraordinary. Torrefaction has been around for a long time, however, to use this process to create a renewable fuel is a new phenomenon. Over the past decade, many inventors have been tinkering with this process in order to create renewable fuel and the key challenges they face when trying to make this process work to generate a fuel are scaleability, mass and energy balance, and cost effectiveness. This patent encompasses a torrefaction solution that is scaleable, does not use more energy to generate the fuel than the fuel can create, and offers a cost effective solution.
  • the torrefaction process requires a heat source operating in a range of 200-400°C in a low oxygen environment to minimize the release of toxic emissions and to avoid complete combustion of the feedstock.
  • the process removes moisture within the feedstock through chemical reactions.
  • the end product is a black organic material known as biochar (resembles charcoal).
  • the biomass is dried and continues with further heating in which more moisture is removed due to the chemical reactions occurring within the hemicellulose and cellulose of the biomass through a thermo-condensation process. As the temperature increases past 160°C, C0 2 is formed. Between 180°C and 270°C, the reaction becomes exothermic and the hemicellulose breakdown continues (Tumuluru, Sokhansanj, Wright and Boardman, 2010).
  • hemicellulose is the primary lignocellulosic material within the feedstock that is degraded into gases (including H 2 , CH 4 , aromatics, CO,C0 2 and C x H y ), condensable liquids (including acids, ketones, furans, alcohols, terpenes, phenols, waxes, tannins, water), and solids (including char, new and existing sugar structures, and new polymers and ash (NRCan - Madrali, 2011).
  • gases including H 2 , CH 4 , aromatics, CO,C0 2 and C x H y
  • condensable liquids including acids, ketones, furans, alcohols, terpenes, phenols, waxes, tannins, water
  • solids including char, new and existing sugar structures, and new polymers and ash
  • Torrefaction is considered to be a mild form of pyrolysis.
  • Table 1 compares the products generated from dry wood using different modes of pyrolysis. With torrefaction, 82% of the product is a solid char and 18% gases are released during the process.
  • the product will maintain 50 to 70% of the mass of the feedstock, but 90% of the energy.
  • the properties of the feedstock biomass are improved through limited devolatilisation that occurs under these conditions.
  • the end product is a biochar that has the potential to replace coal. This biochar end product has increases in caloric value, hydrophobicity, and energy density when compared to the raw feedstock. All of the biomass undergoes dehydration reaction which destroys the -OH groups that are responsible for hydrogen bonding with water therefore the absorption of water is reduced in the densified torrefied product.
  • Table 2 provides the data of key fuel characteristics of a variety of feedstocks (wood versus coal versus charcoal versus torrefied pellets). As can be seen the torrefied pellets have similar caloric value (GJ/t), bulk density, and volumetric energy density as charcoal and coal which is significantly higher than the raw wood.
  • Budarin US2011/0219679 a method for heating the feedstock using microwaves is presented.
  • One disadvantage of microwave-based torrefaction processes is that while they may be quick, they require substantially dry feedstock at elevated temperatures as the input. This requires significant energy in the processing of the biomass.
  • Budarin proposes the agglomeration of feedstock into either pellets or extruded logs which adds costs to the construction and operation of the process.
  • An object of the present invention is to provide a system and process for conversion of organic matter into torrefied product.
  • a system for conversion of organic matter feedstock into a torrefied product the system for conversion of organic matter into a torrefied product, the system comprising a direct fired rotary kiln, the kiln having a first end and a second end, the kiln being tilted at an angle such that the first end is lower than the second end, a burner assembly located at the first end of the kiln, a feedstock input means and a gas conduit located at the second end of the kiln, and a torrefied product outlet at the first end of the kiln.
  • a process for conversion of organic matter feedstock into a torrefied product in a direct fired rotary kiln comprising the steps of: introducing the feedstock into the rotary kiln; applying heat to the feedstock for a residence time sufficient to convert the feedstock to the torrefied product; and collecting the torrefied product.
  • Figure 1 is a schematic illustration of a system in accordance with one embodiment of the present invention.
  • Figure 2 is a schematic illustration of a temperature gradient in a rotary kiln during the torrefaction process in accordance with one embodiment of the present invention.
  • FIG 3 illustrates examples of the feedstock prior to torrefaction 4(a), partially torrefied feedstock 4(b) and completely torrefied final product 4(c).
  • Figure 4 is a graphical plot of refractory and flue gas temperatures along the length of the kiln from (feeder end) to A (burner and discharge end) for tests 1 through 4.
  • Figure 5 is a graphical plot of extrapolated values for natural gas consumed by the afterburner (kg/h) compared to internal temperature (°C) for tests 1 to 4.
  • biomass feedstock including but not limited to wood products (bark, chips, slash), switchgrass, paper products, human and/or animal wastes, de-inking sludge, agricultural residues, construction and demolition waste, and other organic materials.
  • the present invention provides a torrefaction system comprising a direct-fired, refractory-lined, continuously operating rotary kiln. Accordingly, the present torrefaction system also comprises a burner assembly comprising a primary combustor and one or more gas inlets, wherein the burner assembly produces hot, low oxygen content combustion gases that come in direct contact with the feedstock.
  • the control of the internal environment of the kiln creates a steady and stable process that is highly repeatable.
  • the use of the kiln removes critical scaling issues faced by alternative technologies.
  • the rotary kiln design allows for continuous input of the feedstock, and by rotating it, the feedstock is well mixed.
  • the degree of the incline and the speed of rotation control the mixing and the residence time of the feedstock and ensures that there is a consistent end product generated.
  • the presently disclosed system therefore also provides continuous operation.
  • the primary combustor can be fired by a variety of fuels (such as natural gas, propane, diesel or designed to accommodate use of some of the biomass feedstock as a fuel source) and is used primarily for heating of the kiln during initial start-up. Flue gas recirculated from the afterburner at the exhaust of the kiln will provide hot gases during normal operation that will reduce the load on this burner.
  • fuels such as natural gas, propane, diesel or designed to accommodate use of some of the biomass feedstock as a fuel source
  • Direct contact between the hot gases passing through the kiln, the heated refractory, and the feedstock biomass in a controlled low 0 2 environment provides very efficient heating of the feedstock and causes the moisture and volatile organic compounds (VOCs) in the feedstock to vaporize and produce a low to medium BTU gas.
  • This gas can be combusted in an afterburner at the kiln exhaust and the resulting flue gas can supply some of the heat and maintain the low 0 2 environment required to support the torrefaction process in the kiln.
  • the system further comprises an afterburner assembly, immediately downstream of the kiln exhaust, which operates at a slightly negative pressure to prevent flue gas leakage, and completes the burnout of any residual tars and/or other volatiles released during the torrefaction process.
  • the resulting flue gas can then be recirculated through a flue gas recirculation (FGR) system to the input of the kiln to supply heat and maintain the low 0 2 environment required to support the torrefaction process in the kiln.
  • FGR flue gas recirculation
  • the presently disclosed system optionally employs a flue gas recirculation (FGR) loop using these produced gases.
  • FGR flue gas recirculation
  • the low 0 2 environment can be maintained, and the internal kiln temperatures can be controlled (hot gases circulating through the kiln between 500-950°C; and refractory temperature maintained between 200-300°C).
  • the flue gas then is passed through a heat-exchanger (to cool the gases to protect the gas clean-up equipment) and gas clean-up train downstream of the afterburner.
  • the back-end emission control technology is industry standard equipment (e.g. cyclones, baghouse filters etc.).
  • the FGR system also connects to a stack which is required to vent the flue gases in the event of system upset conditions.
  • the torrefied end product of the presently disclosed process is an energy-dense carbon neutral fuel that resembles coal in a number of its properties (black charcoal pieces).
  • the product is more energy-dense, more resistant to water, and more chemically and physically uniform than the feedstock used to make it.
  • the coproduct, or fines, produced also has potential value as a soil amendment product that also acts as a carbon sequestration process, returning carbon to the forest floor or agricultural field.
  • the presently disclosed process is scaleable, and can be used with both a wide variety of feedstocks, and feedstocks with wide variations in physical and chemical properties.
  • the rotary kiln 100 is formed of steel and insulated refractory material, and is provided with internal baffles to ensure mixing of the feedstock when rotated.
  • the kiln is oriented at an angle, wherein the feedstock input assembly is located at the raised end, and the torrefied product output is located at the opposite, lower end.
  • the orientation (i.e., tilt) and the rotational speed of the kiln are controlled to ensure that there is sufficient residence time of the biomass feedstock within the kiln to complete the torrefaction process.
  • the rotational speed and tilt are adjustable, and therefore the residence time is customizable according to the specific biomass feedstock.
  • the feedstock travels through the kiln through the different temperature zones ( Figure 2).
  • the temperature gradient within the kiln is such that the first part of the material's journey is significantly less hot than the burner end, where it is discharged.
  • This cooler section serves to dry the feedstock before torrefaction begins.
  • the lower temperature introduction also encourages early de-volatilisation, which prevents offgasing too close to the burner, which could cause a combustion risk if the oxygen concentration is too high within the kiln.
  • the present system by controlling the time spent in each stage of the process, safely allows the drying, devolatilisation, and torrefaction steps to occur in a single unit, which is more cost effective than running three separate processes.
  • the torrefaction process is complete, and the product is discharged through the torrefied product outlet 110 located at or adjacent to the burner end of the kiln.
  • the outlet is configured to minimize oxygen ingress to the kiln, thereby maintaining a low 0 2 environment conducive to the torrefaction process.
  • the feedstock is introduced to the kiln through a feedstock input assembly 140.
  • the feedstock input assembly can be configured for continuous inputs, which allows the process to be run in a continuous manner.
  • the rate at which the feedstock is introduced is also controllable. It is also within the scope of the presently disclosed system to provide the feedstock in a batch-wise manner, as long as it is in a sufficient frequency and volume that the torrefaction process in the kiln is allowed to proceed in a continuous manner.
  • the feedstock input assembly 140 can employ a screw-type or auger mechanism, conveyor belt system or any other suitable mechanism for continuous feedstock inputs.
  • a burner assembly 120 that produces the hot combustion gases that come in direct contact with the feedstock to drive the torrefaction process.
  • the burner assembly 120 is in communication with a heated gas inlet 180 located at the burner end of the kiln 100.
  • the burner assembly 120 is comprised of a primary combustor fuelled by an external fuel such as natural gas; and optional flue gas injection ports located at the burner combustion zone which permit flue gas to be introduced to the kiln through the burner assembly.
  • natural gas and oxygen inlets are provided to control the amount of heat provided by the burner, which controls the temperature in the kiln.
  • the burner is designed to operate with fuel and air flows that will maintain the appropriate heating, but also a low gas velocity, in the kiln.
  • flue gases which include non-oxidizing gases such as C0 2 and N 2 , allows control of the composition of the gases in the kiln to maintain the low 0 2 environment required for torrefaction (i.e. minimizing the amount of oxidizing gases present).
  • the recirculated flue gas also provides heat to the kiln, minimizing the use of external fuel to support the torrefaction process.
  • Inert gases such as C0 2 or N 2 can also be introduced through dedicated gas inlets located at or near the burner to maintain the internal kiln environment in a safe, non-combustible mode until feedstock can be removed from the kiln during upset conditions.
  • the burner assembly 120 is configured in such a manner that the material inside the kiln will be shielded from direct exposure to the burner flame. This is done to prevent local heating and combustion of feedstock particles at the incoming end of the kiln.
  • the presently disclosed process achieves this by including angled piping between the primary combustor and the heated gas inlet of the kiln.
  • the burner assembly comprises a 90-degree angle in the burner assembly piping prior to the hot gases entering the kiln.
  • Other configurations and piping shapes which prevent direct exposure of the burner flame to the interior of the kiln are within the scope of the present invention.
  • Other methods of preventing direct exposure include incorporation of internal baffles or shielding at the burner end of the kiln to absorb the radiation from the burner flame.
  • Combustion gases from the burner travel through the kiln, picking up the moisture and volatiles from the feedstock.
  • the resulting gaseous mixture then moves through a transition box/gas conduit 150 to the afterburner 160, where the volatiles are burned.
  • the resulting flue gas is then processed through a flue gas recirculation system, which includes heat-exchange equipment (to cool the gas to protect the emission control equipment) and emission control equipment downstream of the afterburner (as shown in Figure 1).
  • the back-end emission control technology is industry standard equipment (e.g. cyclones, baghouse filters etc.).
  • the FGR system also connects, downstream of the baghouse filters, to a stack which is required to vent the flue gases in the event of system upset conditions.
  • the flue gas is drawn through the FGR system by an Induced Draft Fan after the baghouse filters and is normally sent through a condenser to remove water from the flue gas. This dry cool flue gas is then recirculated back to the burner assembly into the kiln via the heating side of the heat-exchange equipment in the FGR, thereby providing heated flue gas for injection at the burner assembly.
  • the gas conditioning suite comprises the afterburner 160, a cyclone 171, baghouse 172, an optional scrubber 173, an ID fan 174, a condenser (not shown), a stack 175, and a heat exchanger 176. Any or all of these may exist in multiples.
  • Continuous emissions monitoring (CEM) is conducted at the baghouse (CO, C0 2 , S0 2 , NO x , and 0 2 ).
  • the emission control equipment comprises a cyclone, baghouse filter, an ID fan, and a stack as shown in Figure 1. The purpose of the emission control equipment is to clean the flue gas to ensure it can be released to atmosphere by meeting the local air emissions standards.
  • Emissions monitoring can be conducted at the baghouse (CO, C0 2 , S0 2 , NO x , and 0 2 ) or at the stack.
  • the gas conditioning suite includes heat exchanger(s) and a water vapour condenser(s).
  • the water vapour condenser is employed to remove water vapour in the flue gas before returning the flue gas to the kiln.
  • the heat exchanger (s) function is to first cool the flue gas to the required temperature to permit it to enter the emission control equipment without damaging it, and then to reheat the dry, clean flue gas returning from the water vapour condenser before injecting it back into the kiln at the re-injection ports in the burner assembly.
  • Heat exchangers may exist in multiples and their arrangement will depend on the numbers of emission control equipment in the FGR.
  • the present torrefaction system further comprises a control subsystem, which includes, for example, sensors throughout for measuring kiln rotation speed, fuel flow, temperature at burner, temperature in kiln (gas and refractory), 0 2 sensor, and standard emissions monitoring (e.g. particulate matter, CO, NO x , SO x , etc.).
  • the kiln rotation speed is used to control material residence time.
  • the fuel flow controls the burner heat input and the gas temperature entering the kiln, and therefore also the temperature of the refractory.
  • the gas monitoring including 0 2 levels, helps ensure the system is sealed and operating safely.
  • the emissions monitoring equipment ensures that the emissions control equipment is working as required.
  • Other sensors are provided to determine gas composition at various points throughout the system.
  • the first test was performed April 21, after several days of becoming acquainted with the system and test-firing the new burner. The primary objective was to try a set of conditions and to see what came out the other end. After the test, additional insulation was added to the outside of the burner and a screen was installed to prevent accidental contact with the hot equipment. The test lasted 3 hours and the difference from one end of the kiln to the other was 125 °C. Torref action occurred only to a very limited extent. The product was not remarkably different than the feedstock. We concluded that the temperature was too low. The highest refractory temperature reached during this test was less than 200 °C, and the retention time was approximately 45 minutes.
  • the second test aimed to improve upon the disappointing product from the first test by increasing the temperature of the flame and kiln refractory.
  • the test lasted 3.5 hours and the difference from one end of the kiln to the other was 161 °C.
  • the product was darker than the product of test 1, but still nowhere near the appearance of coal.
  • the highest refractory temperature reached during this test was less than 245 °C, and the retention time was approximately 45 minutes.
  • Test 3 incorporated the techniques figured out in the first two tests, and further increased the temperature of the flame and kiln refractory. The firing rate was manipulated in order to create a darker product. The product of test 3 is shown in Figure 3(b). The test lasted 4 hours and the difference from one end of the kiln to the other was 152 °C. This test was encouraging because it yielded a dark brown product. The highest refractory temperature reached during this test was less than 255 °C, and the retention time was approximately 45 minutes.
  • Test 1 yielded a product that looked almost unchanged compared to the feedstock. It did not appear to be torrefied at all, but rather had a dirty and grey appearance. The product created in test 2 was darker than what was produced in test 1, but still did not look very different than the feedstock. In test 2, some darker pieces were starting to appear. Products from tests 1 and 2 were not analysed because it was determined visually that the target product had not been successfully created. [0055] Tests 3 and 4 were also successively darker ( Figure 3). The residence time for the first three tests was between 30 and 75 minutes. For the fourth, the rotation was slowed to increase the residence time to approximately two hours. Residence times were estimated based on process output as there were no available means of quantifying the exact residence times.
  • test 4 Another difference for test 4 is that the kiln was pre-warmed. The burner was fired up the night before and the refractory was significantly hotter than for the previous three runs (see Figure 4). The temperature gradient within the kiln was also more significant for test 4, with a 174°C difference from one end to the other.
  • Descriptive Statistics For analytical purposes, a half-hour period of steady state was selected for comparisons between the tests. This half -hour period was used in order to eliminate any inconsistencies that may result from start-up and shutdown operations. Means were calculated using the descriptive statistics tool in MS Excel (Table 3). The elapsed time from the beginning of the test to the start of the half-hour steady state sample's beginning is noted in the third column of Table 3. In each case, it was approximately 2.5 hours after the test started.
  • Burner flue gas 1 (°C) 895.000 961.847 958.512 927.509
  • Burner flue gas 2 (°C) 929.993 1016.654 1001.665 970.927
  • Baghouse NO x (ppm) 12.357 49.462 26.059 30.650
  • Baghouse S0 2 (ppm) 327.214 -0.846 0.294 5.150
  • Baghouse CO (ppm) 1562.167 72.154 0.471 22.800
  • Natural gas was used to fuel the torrefaction process. Flue gas recirculation was simulated by injecting C0 2 and N 2 into the burner very near the natural gas inlet. Natural gas was also used to fuel the afterburner. The flow of natural gas across the whole system (burner and afterburner) was similar during steady state of all four experiments (Table 4). However, the quantity of fuel used by the burner declined sharply from one test to the next. Test 4 used the least natural gas and N 2 , and it had a significantly reduced rotation speed. Test 4 accepted the same quantity of feedstock during the steady state period as test 3 (Table 4), despite the longer retention time. In addition, it had a lower temperature than test 3 and produced a more torrefied product.
  • Feedstock (pine chips) and the products from tests 3 and 4 were analyzed using calorimetry (Table 5). Calorimetric analysis was used to determine if there was a significant increase in the energy value of the product compared to the feedstock. Initial estimates were that an increase of 100% was possible. This was not achieved when compared on a dry basis. However, the dried product from test four had double the BTU value of the "as received" wood chips (Table 5).
  • the feedstock had more moisture than expected, and therefore it is useful to note that a feedstock that has greater than 40% moisture can be successfully torrefied with the present system.
  • Table 5 Analytical results for calorimetry of untreated wood chips, the product from test 3, and the product from test 4.
  • EXAMPLE 5 [0063] Sieve analysis separated the product from test 4 into five standard ASTM size categories (ASTM D4749). Each size underwent calorimetric analysis to test the thoroughness and uniformity of torrefaction. Most pieces of product were found to be smaller than a half inch, with only about 13% exceeding 1 ⁇ 2". A significant quantity of very small pieces made it through, supporting the claim that the draft inside the kiln is not causing all small particles to be blown into the afterburner. The size distribution analysis results and the corresponding energy values for the test 4 product are presented in Table 6.
  • Table 7 Proximate analysis results presented as percentage of total mass for untreated wood chips, the product from test 3, and the product from test 4.
  • Test 3 received 4.12 0.82 77.23 17.83 0.01
  • Test 4 received 38.5 1.42 41.66 18.41 ⁇ 0.01
  • Table 8 Ultimate analysis results presented as a percentage of total mass for untreated wood chips and the products of tests 3 and 4.
  • Test 3 received 4.12 52.83 5.61 0.82 0.14 0.01 36.47
  • Test 4 received 38.5 36.61 2.15 1.42 0.08 ⁇ 0.01 21.22

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  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
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  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Sustainable Development (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Dispersion Chemistry (AREA)
  • Muffle Furnaces And Rotary Kilns (AREA)
  • Processing Of Solid Wastes (AREA)
  • Drying Of Solid Materials (AREA)
  • Meat, Egg Or Seafood Products (AREA)
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Abstract

La présente invention porte sur un système pour la conversion de matière organique en un produit torréfié, le système comprenant un four rotatif à chauffage direct.
EP20120807598 2011-07-07 2012-07-06 Système et procédé pour la conversion de matière organique en produit torréfié Withdrawn EP2729749A4 (fr)

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PCT/CA2012/050457 WO2013003960A1 (fr) 2011-07-07 2012-07-06 Système et procédé pour la conversion de matière organique en produit torréfié

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PL404037A1 (pl) * 2013-05-22 2014-11-24 Boneffice Spółka Z Ograniczoną Odpowiedzialnością Sposób prowadzenia procesu toryfikacji biomasy, instalacja do prowadzenia procesu toryfikacji biomasy, toryfikowana biomasa oraz sposób oczyszczania gazów wylotowych z procesu toryfikacji
CN105199762A (zh) * 2014-06-25 2015-12-30 中国石油大学(华东) 回转窑煤热解制焦油、半焦、煤气的系统
EP3037765A1 (fr) * 2014-12-26 2016-06-29 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Fours rotatifs à contre-courant inclinés à combustion directe et leur utilisation
AT519471B1 (de) * 2017-02-06 2018-07-15 Herz Energietechnik Gmbh Verkohlungsanlage
FR3075196B1 (fr) * 2017-12-15 2019-11-15 Fives Fcb Installation de production de clinker et procede de production de clinker dans une telle installation
CA3105525A1 (fr) * 2018-07-23 2020-01-30 Debris Diversion Solutions Procedes ameliores de reduction de volume de decharges
CA3140281A1 (fr) 2019-06-07 2020-12-10 Torrgreen B.V. Reacteur et procede de torrefaction
JP7416654B2 (ja) * 2020-03-30 2024-01-17 日鉄エンジニアリング株式会社 改質石炭の製造方法および製造設備
CN114110619B (zh) * 2021-11-12 2024-07-16 中国恩菲工程技术有限公司 污泥干化焚烧一体化处理装置及方法
FR3129614A1 (fr) 2021-11-29 2023-06-02 Commissariat A L'energie Atomique Et Aux Energies Alternatives Installation et procédé afférent de production de granulés de biomasse hydrophobes.

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US20030221363A1 (en) * 2002-05-21 2003-12-04 Reed Thomas B. Process and apparatus for making a densified torrefied fuel
US20090229500A1 (en) * 2008-03-14 2009-09-17 Massey Sammy K Animal carcass incinerator
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US20140166465A1 (en) 2014-06-19
BR112014000123A2 (pt) 2017-03-28
EP2729749A4 (fr) 2015-04-08
WO2013003960A1 (fr) 2013-01-10

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