WO2015102480A2 - Appareil permettant de produire des biocarburants à partir de biomasse - Google Patents

Appareil permettant de produire des biocarburants à partir de biomasse Download PDF

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Publication number
WO2015102480A2
WO2015102480A2 PCT/MY2014/050014 MY2014050014W WO2015102480A2 WO 2015102480 A2 WO2015102480 A2 WO 2015102480A2 MY 2014050014 W MY2014050014 W MY 2014050014W WO 2015102480 A2 WO2015102480 A2 WO 2015102480A2
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WO
WIPO (PCT)
Prior art keywords
biomass
cyclone structure
reaction chamber
combustion chamber
bio
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PCT/MY2014/050014
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English (en)
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WO2015102480A3 (fr
Inventor
Sim Tee @ Tang Hai Chiang Tan
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Regenergy Technologies Sdn Bhd
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Publication of WO2015102480A2 publication Critical patent/WO2015102480A2/fr
Publication of WO2015102480A3 publication Critical patent/WO2015102480A3/fr

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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
    • C10B49/02—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
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • Fossil fuels have always been a dominant source for global energy consumption which increases at a substantial rate with growth of population and industrialization.
  • Today, depletion of fossil energy resources and generation of greenhouse gases due to excessive consumption of fossil fuels have caught global attention to seek for alternative energy resources which are sustainable and environmentally friendly.
  • Biomass arises as a promising energy resource to supplement fossil fuels, due to its abundant amount.
  • biomass refers to carbon based organic materials produced by photosynthesis.
  • the carbonaceous compounds contained in the biomass can be converted thermally to generate energy.
  • Examples of biomass include but are not limited to terrestrial vegetation, residues from forestry or agriculture, animal wastes and municipal wastes.
  • Biomass consists of three types of polymeric components which are cellulose, hemicellulose and lignin. It can be converted by a thermal conversion process either in absence of oxygen or in oxygen-limiting condition to different forms of fuels, such as bio-char, bio-oil or combustible gas also known as producer gas.
  • biomass undergoes a partial pyrolysis process known as torrefaction, in which lignocellulose structure is depolymerised and devotalised along with release of pyroligneous acids, water, and non-condensable gases (carbon monoxide (CO), carbon dioxide (C0 2 ));
  • torrefaction a partial pyrolysis process known as torrefaction, in which lignocellulose structure is depolymerised and devotalised along with release of pyroligneous acids, water, and non-condensable gases (carbon monoxide (CO), carbon dioxide (C0 2 ));
  • hemicellulose the most reactive component, is almost completely devolatilised and depolymerized at temperatures ranging from 200 to 300°, whilst cellulose and lignin are depolymerised and devolatilised at 300 to 400°C and 250 to 500°C respectively.
  • the liquid fuel vapour is converted to combustible gases through a redox process or a combined oxidation-reduction process under sub-stoichiometric conditions known as gasification in which char reacts with carbon dioxide and steam to produce carbon monoxide, hydrogen and trace of methane.
  • gasification in which char reacts with carbon dioxide and steam to produce carbon monoxide, hydrogen and trace of methane. The reactions occur at temperatures above 650°C.
  • Torrefaction of biomass is a process in which the biomass is heated at a temperature ranging from 200 to 350°C in oxygen-limiting condition.
  • the biomass can either be heated directly using a gaseous heating medium such as inert gases, superheated steam, or be heated indirectly through contact with a hot surface.
  • the heating results in devolatilisation and depolymerisation of major components of the biomass (hemicellulose, cellulose and lignin) and weight loss in biomass due to emission of moisture, volatile hydrocarbon and some gases.
  • Resultant torrefied biomass or bio-char which is a dry, brittle and darkened material, has an enhanced energy value measured in terms of heat energy per unit of weight.
  • Gaseous or liquid fuels can be produced by fast pyrolysis of biomass.
  • biomass is heated rapidly to temperatures between 450 to 650°C in absence of oxygen to convert its volatile matters into vapour which can be condensed to form liquid bio-oil.
  • Various types of reactors have been developed for such objective and known as Bubbling-Fluidized Bed Reactor, Circulating-Fluidized Bed Reactor, Rotating Cone Reactor, Auger Reactor and Ablative Reactor. These reactors are designed based on different principles and some may also require external transport of hot sand as heating medium and mechanical means to remove solid residues.
  • gasification of biomass is a thermochemical process which converts volatile matters of biomass materials into combustible gas known as producer gas at temperature above 650°C under sub-stoichiometric condition.
  • the producer gas contains mainly nitrogen, carbon dioxide, oxygen, carbon monoxide, hydrogen and trace of methane.
  • various types of apparatus have been developed and can be classified into fixed bed gasifier, fluidized bed gasifier and cyclonic gasifier. Nevertheless, there are certain disadvantages in these gasifiers, despite the fact that they are widely applied in the industries.
  • the fixed bed gasifier is restricted in capacity by its slow conversion rate, bulky volume and up-scaling limit for uniform temperature distribution.
  • a biomass gasifying device is disclosed in China Patent Publication No. 201010626. It claims a cylindrical biomass gasifying device having an upper and a lower chamber separated by a conical funnel.
  • a funnel-shaped helical gas distribution furnace bridge is hung on the funnel opening of a conical funnel on the upper chamber, whereas an inner furnace cylinder with a material guide hole and a conical cover with a gas guide hole is provided at the bottom of the concentrical cover base of the air distribution furnace bridge. It is also disclosed that a gasifying agent inlet port is provided in the cavity of the lower chamber, while a water sealed scum pipe is provided at the bottom of the lower chamber.
  • the apparatus includes a cylindrical shaped upper portion and a tapered shaped lower portion.
  • the cylindrical shaped upper portion is an integrated combustion and gasification chamber and the tapered shaped lower portion serves as a gasification chamber.
  • a splash board is set at the upper portion of the cylindrical shaped gasification chamber and smoke outlet is mounted on the top.
  • a fuel inlet is mounted tangentially onto the cylindrical shaped upper portion.
  • a resistant wire igniter is located in fuel inlet, whereas a steam inlet is disposed in center portion of the tapered shaped gasification chamber.
  • An ash outlet is disposed at bottom.
  • the compact apparatus is, preferably, consisting of a reaction chamber defined by an integral space formed from a double cyclone structures (i.e. an outer and an inner cyclone structures) and a combustion chamber located underneath the reaction chamber.
  • the thermal conversion process taking place in the apparatus can be enhanced as result of rapid and vigorous mixing resulted from a cyclonic motion of a vortex generated therein.
  • the walls of the apparatus can also be easily heated up to a predetermined temperature by heat generated from combustion of biomass in the combustion chamber and which passes through rectangular perforations fabricated in an annular base plate disposed at bottom of the outer cyclone structure of the reaction chamber.
  • the invention aims to provide an apparatus capable of performing thermal or thermochemical conversion processes for torrefaction, fast pyrolysis and gasification under different operating conditions. It is desirable that the apparatus is simple in structure with no moving parts to minimize maintenance cost. It is also desirable that the apparatus is integrated with a programmable logic controller (PLC) system for easy operation and effectively controlling temperature, pressure and air/fuel ratio to maintain a stable and consistent operating condition during the thermal conversion process.
  • PLC programmable logic controller
  • One of the aspects of the invention is to develop an apparatus capable of performing thermal or thermochemical conversion processes, including but not limited to torrefaction, pyrolysis and gasification under different operating conditions and scaling up for commercial production.
  • Another aspect of the invention is to provide an apparatus which enables effective control of temperature, pressure and air/fuel ratio to maintain a stable and consistent operating condition by a programmable logic controller system.
  • a further aspect of the invention is to develop an apparatus that enhances the heat transfer rate to the feedstock by vigorous abrasion against the heated walls of the apparatus under the action of the centrifugal force generated by the cyclonic motion of vortex generated inside the apparatus.
  • Still another aspect of the invention is to provide an apparatus which is simple in structure with no moving parts to minimize subsequent maintenance cost.
  • Yet another aspect of the present invention is to provide an apparatus that provides longer residence time to allow relatively coarser particle sizes of biomass feedstock (up to -25 mm) for torrefaction, pyrolysis and gasification processes.
  • the embodiment of the present invention describes an apparatus for producing fuels from biomass comprising:
  • a reaction chamber defined by the integral space formed from an outer inverted cyclone structure having a cylindrical sidewall, an annular base plate fabricated with a radial array of rectangular perforations and a substantially tapered top and an inner cyclone structure having a cylindrical sidewall, an open top and a substantially tapered bottom section with an end exit opening;
  • the outer and inner cyclone structures are arranged in such a way that the inner cyclone structure is enclosed coaxially within the outer inverted cyclone structure and the tapered bottom section of the inner cyclone structure extends downwards through the annular base plate; a tubular outlet extending from the tapered top into the upper portion of the inner cyclone structure;
  • a feed inlet is mounted tangentially onto the sidewall of the outer cyclone structure above to the annular plate for infeed of biomass feedstock by high speed blown gas; wherein the biomass feedstock is heated up to a preset temperature rapidly on contacting the hot walls to set off thermal conversion process to produce fuel products.
  • the mixture of air/gas, products and unconverted biomass forms a vortex and swirls upwards inside the outer cyclone structure and then downwards into the inner cyclone structure through the open top upon reaching the tapered top of the outer cyclone structure.
  • the biomass feedstock is kept in constant collision and abrasion with the hot walls under the action of centrifugal force generated by the cyclonic motion of vortex and heated up to the selected temperatures to set off thermal or thermochemical conversion process to produce biofuels in solid, liquid vapor and gaseous forms.
  • the solid product or remnants such as ash or char are collected and discharge through the opening at the bottom of inner cyclone structure into the waste collection system and the gaseous products swirl upwards from the tapered bottom of the inner cyclone structure and finally exit through the outlet pipe at the top;
  • a combustion chamber which is defined by the sidewalls of an inner and an outside cylindrical structures, a bottom supporting base and is disposed underneath the reaction chamber to surround the sidewall of the extended tapered bottom section of the inner cyclonic structure; a feed inlet is mounted tangentially onto the sidewall of the outer cylindrical structure for infeed of biomass feedstock by high speed blown gas into the combustion chamber; wherein the biomass feedstock is combusted to generate and supply heat to the reaction chamber through the perforations in the annular plate required for the thermal or thermochemical conversion processes.
  • the combustion chamber is maintained at a temperature not exceeding 800°C to substantially prevent fusion of the ash formed during combustion from damaging the internal walls of the combustion chamber.
  • the apparatus is integrated with a programmable logic controller (PLC) system for automated operation and effective control of operating parameters, viz., temperature, pressure and air/fuel ratio to maintain a stable and consistent operating condition during the thermal conversion process.
  • PLC programmable logic controller
  • the air/fuel ratio in the present invention refers to ratio of biomass feedstock to air, in which the air may be a combination of fresh air and composition of the gas recovered from the condenser.
  • the apparatus further comprises a waste collection assembly consisting of a rotary valve feeder and a water-cooled screw conveyor connected to the opening at the bottom of the inner cyclone structure for removal of the discharged solid product or remnants.
  • the apparatus further comprises a heat insulating layer enclosing the outer cyclone structure.
  • the heat insulating layer is preferably a layer of mineral wool to minimize heat loss and maintain the temperature within the apparatus.
  • the heat insulating layer is enclosed by a cylindrical hollow metal casing which serves as a protection shell for the apparatus.
  • the cylindrical hollow metal casing is made of mild steel.
  • the apparatus further comprises:
  • a first feeding system for the reaction chamber having a biomass feedstock storage hopper mounted with a rotary valve feeder at its bottom; an ejector is installed underneath the rotary valve feeder to inject biomass feedstock into the reaction chamber through the air/gas pipe connected to the feed inlet; a high pressure blower draws fresh air and flue gas from the exhaust outlet of the apparatus to inject through the feed inlet into the reaction chamber to serve as feedstock carrier medium.
  • the flow rates of air and flue gas are regulated by electromagnetic actuator valves and measured by flow sensors;
  • a second feeding system for the reaction chamber having a biomass feedstock storage hopper mounted with a rotary valve feeder at its bottom; an ejector is installed underneath the rotary valve feeder to inject biomass feedstock into the combustion chamber through the air/gas pipe connected to the feed inlet; a high pressure blower draws fresh air and flue gas from the exhaust outlet of the apparatus to inject into the combustion chamber through the feed inlet.
  • the flow rates of air and flue gas are regulated by electromagnetic actuator valves and measured by flow sensors;
  • Figure 1 shows a front elevational view of the apparatus, according to the
  • Figure 2 shows the isomeric view of an annular plate having a radial array of rectangular perforations, according to the preferred embodiment of the invention.
  • Figure 3 shows a top sectional view of the apparatus along the dashed cutting plane line A- A'.
  • Figure 4 shows a sectional view of the apparatus along the dashed cutting plane line B-B'.
  • Figure 5 shows a sectional view of the apparatus along the dashed cutting plane line C-C * .
  • Figure 6 shows a schematic diagram illustrating operation of the apparatus and the ancillary equipment, according to the preferred embodiment of the invention.
  • This invention relates to an apparatus for producing fuels from biomass.
  • the invention relates to an apparatus for producing fuels from biomass, in which enhanced thermal or thermochemical conversion process is achieved by rapid and vigorous mixing resulted from the action of centrifugal force generated by the cyclonic motion of vortex generated therein.
  • this invention discloses an apparatus for producing fuels from biomass comprising:
  • a reaction chamber (101b, 105) defined by an integral space formed from an outer inverted cyclone structure (101b), defined by a cylindrical sidewall (102b), an annular base plate (136) fabricated with a radial array of rectangular perforations and a substantially tapered top (104), and an inner cyclone structure (105), having a cylindrical sidewall (106b), an top opening (107) and a substantially tapered bottom section (106a) with an end exit opening (109); wherein the outer and inner cyclone structures are arranged in such a way that the inner cyclone structure is enclosed coaxially within the outer cyclone structure and the tapered bottom (106a) of the inner cyclone structure extends downwards through the annular base plate (136); a tubular outlet (108) extending from the tapered top (104) into the top opening of the inner cyclone structure (107); a first feed inlet (124) mounted tangentially to the sidewall of the outer cyclone structure (102b) above to the annular plate (136) for in
  • a combustion chamber (101a) having a cylindrical structure which is defined by the sidewalls of an inner cylindrical structure (106a), an outer cylindrical structure (102a) and a bottom supporting base (103) and disposed underneath the reaction chamber (101b) to surround the extended tapered bottom section (106a) of the inner cyclone structure; a second feed inlet (134) mounted tangentially to the sidewall of the outer cylindrical structure (102a) above to the supporting base (103) for infeed of biomass feedstock by high speed blown gas delivered by a high pressure blower (137); wherein biomass is combusted to generate and supply heat to the reaction chamber (101b, 105) through the perforations in the annular base plate (136) required for thermal or thermochemical conversion processes in the reaction chamber;
  • the combustion chamber is maintained at a temperature not exceeding 800°C to substantially prevent fusion of the ash formed during combustion from damaging the internal walls of the combustion chamber.
  • the apparatus further consists of a waste collection assembly, comprising of a rotary valve feeder (114) installed beneath the second opening (109) of the cyclone reactor (105) and a water-cooled discharging screw conveyor (115) connected to the outlet of rotary valve (114).
  • the solid remnants such as ash and char discharged through the rotary valve feeder (114), are cooled and transferred to the waste chamber (116) via a water-cooled discharging screw conveyor (115).
  • the solid remnants in the combustion chamber (101a) can be discharged through the exit (135) at the base to avoid accumulation of unwanted solid remnants.
  • the apparatus further comprises a heat insulating layer (113a) enclosing the sidewalls of the outer cyclone structure (102a, 102b).
  • the heat insulating layer is preferably a layer of mineral wool to minimize heat loss and maintain the temperature within the apparatus.
  • the heat insulating layer is further enclosed by a cylindrical hollow metal casing (113) which serves as a protection shell for the apparatus.
  • the cylindrical hollow metal casing is made of mild steel.
  • the walls (102, 106b) of the combustion and reactions chambers are built with refractory material or high temperature alloys which are able to retain its strength at temperatures as high as 1200°C.
  • the apparatus further comprises:
  • a first feeding system for the reaction chamber having a biomass feedstock storage hopper (110) mounted with a rotary valve feeder (111) at its bottom; an ejector (123) is installed underneath the rotary valve feeder (111) to inject biomass feedstock into the reaction chamber through the air/gas pipe (112) connected to the first feed inlet (124);
  • a high pressure blower (125) draws flue gas from the exhaust outlet (108) of the apparatus after being cooled in a cooler/condenser (145) and also fresh air to provide an air/gas flow which serves as carrier medium through the ejector (123), inlet pipe (112) and feed inlet (124) into the reaction chamber (101b).
  • the flow rates of air and flue gas are regulated by electromagnetic actuator valves (120, 126) and measured by flow sensors (121, 127); (b) a second feeding system for the combustion chamber having a biomass feedstock storage hopper (128) mounted with a rotary valve feeder (129) at its bottom; an ejector (131) is installed underneath the rotary valve feeder (129) to inject biomass feedstock into the combustion chamber (101a) through the air/gas pipe (132) connected to the feed inlet (134); A high pressure blower (137) draws fresh air and flue gas from the exhaust outlet (108) of the apparatus after being cooled in the cooler/condenser (145) and also fresh air to provide an air/gas flow which serves as carrier medium through the ejector (131), inlet pipe (132, 133) and feed inlet (134) into the reaction chamber (101b).
  • the flow rates of air and flue gas are regulated by electromagnetic actuator valves (138, 140) and measured by flow sensors (139, 141).
  • the biomass stored in the storage hoppers (110, 128) can be, but not limited to, wood chips, coffee grounds and crushed oil palm fiber.
  • the biomass feeds are preprocessed in pulverized form such that the biomass could be conveyed pneumatically by the air/gas carrier medium during the thermal conversion process. Sizes of the biomass feed particles up to 25 mm are allowed so as to reduce the material grinding cost. Nevertheless, the particle size is not limited thereto as it depends on the physical properties of the biomass feeds and speed of the air swirling inside the apparatus.
  • the pulverized biomass feeds are pre-dried to a moisture content less than 15% before it is delivered to the storage hoppers (110, 128);
  • the flue gas or gaseous products enter the cyclone dust collector where the fine solid particles are collected and discharged through the outlet (143);
  • a water cooled condenser (145) having its inlet connected to the exit of cyclone dust collector (144) for cooling the flue gas, producer gas down to 80°C and condensing steam to water or fuel vapour to liquid bio-oil.
  • the apparatus works in collaboration with a programmable logic controller (PLC) system for automated operation and effective control of the operating parameters, viz., temperature, pressure and air/fuel ratio to maintain a stable and consistent operating condition during the thermal conversion process.
  • PLC programmable logic controller
  • the air/fuel ratio in the present invention refers to ratio of biomass feedstock to air, in which the air may be a combination of fresh air and composition of the gas recovered from the condenser.
  • a number of measuring devices are added to the apparatus for optimization of operation by effective controlling and monitoring the process variables, such as but not limited to, temperature, pressure, blown gas flow rate and biomass feeding rate.
  • thermocouples 117a, 117b
  • a pressure sensor 117b is installed at the outlet (108) to measure the pressure at the outlet (108) where flue gas or gaseous product is discharged.
  • the feeding rate of biomass feedstocks to the reaction chamber and combustion chamber can be measured by the rotational speed of the rotary valve feeder by rotary speed encoders (119, 130) mounted onto the shaft of the rotary valve feeders (119, 130).
  • the respective flow rates of air and flue gas are measured by a plurality of flow sensors (120, 121, 127, 139, 141) and regulated by electromechanical actuator valves (120, 126, 138, 140).
  • electromechanical actuator valves are located before the flow sensors.
  • All sensors are connected to the input terminals of a programmable logic controller (PLC), where output signals from the sensors are processed according to a pre-defined algorithm for optimizing the combined operations of the apparatus by monitoring and controlling the process variables, namely, temperature, pressure and air/fuel ratio (referred to as ratio of mass flow rate of air to that of biomass feedstock) through regulating the rotational speed of the rotary valve feeders (111, 129) and the deflection angle of the electromechanical actuator valves (120, 126, 138, 140) with output signals from the PLC.
  • PLC programmable logic controller
  • the combustion chamber (101a) is heated to a first temperature, preferably 300°C, using an oil or gas burner mounted at the inlet (134).
  • a first temperature preferably 300°C
  • the biomass feedstock which is pre-processed by pulverizing to sizes less than 25mm and pre-dried to moisture content less than 15% is fed from the storage hopper (128) of the second feeding system to the combustion chamber (101a) through the rotary valve feeder (129).
  • the biomass is injected by a flow of blown gas at speed of 15 to 25 m/s into the bottom section of combustion chamber (101a) through the second feed inlet (134), forming a high-speed vortex of mixture of gas and biomass particles therein.
  • the blown gas is a mixture of air and flue gas.
  • the flue gas which contains mainly carbon dioxide with low oxygen content, is drawn from the exhaust outlet (108) of the apparatus and cooled down to 80 °C in a cooler/condenser (145) before supplying to the combustion chamber (101a) to keep the temperature below 800°C and prevent fusion of ash from damaging the internal walls of the combustion chamber.
  • the flow rate of blown gas can be regulated by the electromagnetic valves (138, 140) which are in turn monitored by the PLC with signals feedback from the flow sensors (139, 141) and thermocouple (117a).
  • the vortex of mixture of air, flue gas and feedstock swirls inside the combustion chamber (101a) and keeps the feedstock in constant collision and abrasion with the heated walls (102a, 106a) under the action of centrifugal force generated by the cyclonic motion of vortex. It thus enhances the heat transfer rate between the feedstock and heated walls.
  • the feedstock ignites when contacts with the heated walls and burns spontaneously.
  • the temperature inside the combustion chamber (101a) is controlled and maintained at a preset value by the PLC by regulating the rotating speed of rotary valve feeder (129) with the signals feedback by the thermocouple (117a) and the rotational speed sensor (130).
  • the PLC also processes the signals from the air flow sensor (139) and the rotational speed sensor (130) by executing an algorithm to keep the air/fuel ratio slightly exceeding 6, depending on the type biomass feedstock, to allow complete combustion in the combustion chamber (101a).
  • the hot gas generated in the combustion chamber (101a) is forced to enter the reaction chamber (101b) through the rectangular perforations in the annular plate (136) to supply heat required by the reaction chamber (101b, 105) for thermal or thermochemical conversion of feedstock therein.
  • the biomass feedstock is fed from the storage hopper (110) through the rotary feeder (111) to the ejector (112) through which the feedstock is injected by an air/gas flow supplied by the high pressure blower (134) through the inlet pipe (112) and first feed inlet (124) into the reaction chamber (101b).
  • the high pressure blower (134) supplies also a flow of air-gas serving as carrier medium of the feedstock into the outer inverted cyclonic reaction chamber (101b) through the inlet pipe (122) and feed inlet (124) at speed of 15 to 25 m/s.
  • a cyclonic vortex of air-gas-biomass mixture is developed and swirls upwards.
  • the upward vortex containing a mixture of gas, solid remnants and possibly some unconverted biomass particulates, is being forced to move downwards into the inner cyclone structure (105) through the top opening (107).
  • the unconverted biomass particulates collide more frequently with the heated cylindrical sidewalls (106a, 106b) to further enhance the thermal conversion rate due to increased swirling speed of vortex in the inner cyclone structure.
  • the solid products, solid remnants such as ash or char are separated from the gaseous products under the action of centrifugal force generated by the cyclonic motion of vortex and discharged through the exit opening (109) of the inner cyclone structure (105) to the discharging screw conveyor (115) and finally into the waste chamber (116).
  • the gaseous product such as non-condensable gases, oil vapor or producer gas reverse its direction to swirl upwards until it finally exits through the outlet (108) at the top of the apparatus.
  • the outlet (108) is having a pressure lower than the inner cyclone structure (105) to allow the gases produced to discharge through it.
  • biomass feedstock On swirling through the reaction chamber, biomass feedstock is kept in constant collision and abrasion with the hot walls (102b, 106b) under the centrifugal force generated by the cyclonic motion of vortex.
  • the actions of collision and abrasion of the biomass against the hot walls enhance the rate of heat transfer and thereby speed up the thermal conversion process and at the same time reduce the sizes of feedstock particulates by scraping away the ash or char formed on the surfaces.
  • the feeding rate of feedstock is so controlled to allow complete thermal or thermochemical conversion on reaching the lower tapered section of the inner cyclone structure (105) wherefrom the vortex reverses in direction and swirls upwards, releasing the gaseous products or non-condensable gases through an outlet pipe (108) while solid products or solid remnants such as ash or char is separated from the vortex and discharged through second opening (109) and rotary valve feeder (114) to the discharging screw conveyor (115).
  • thermochemical conversion processes namely, torrefaction, pyrolysis and gassification
  • PLC which contains well defined instructions for processing and monitoring the process variables according to the requirements of the operating conditions of the apparatus to perform as torrefaction reactor, bio-oil reactor or gasifier.
  • the process variables which include temperature, pressure and air/fuel ratio, are so controlled by the PLC system to maintain consistent product quality and high productivity for performing the three different functions of apparatus:
  • the solid product produced from torrefaction reactor is a partially carbonized solid containing most of the volatile components of the biomass. It is a stable, brittle, water resistant (hydrophobic) and biologically non-degradable in storage.
  • the calorific value varies from 5500 to 6500 kcal/kg, depending on the degree of carbonization of the product.
  • the feedstock is preferred to be torrefied to get rid of moisture and pyro capitaous acid contents.
  • the biomass feedstock being carried along by the vortex, is heated up rapidly by the hot sidewalls (102b, 106b) at a rate of ⁇ 103K/s to 600°C set off the pyrolysis process and releases the volatile matters as liquid vapour as it swirls upwards in the outer cyclone structure (101b).
  • the vortex On reaching the tapered top (104). the vortex reverses its direction downwards and then upwards again upon reaching the tapered section of the inner cyclone structure (105) and finally exits through the outlet pipe (108) as flue gas and oil vapour.
  • the ash and char are separated out from the vortex flow and discharged through the second opening (109) to the rotary valve feeder (114) and water-cooled discharging screw conveyor (115).
  • the flue gas and oil vapors are drawn to the cyclone dust collector (142) where the fine particulates are collected and discharged through outlet (143).
  • the clean flue gas and oil vapour exit through the outlet (144) and enter the cooler/condenser (145) where the oil vapor is condensed to bio-oil and discharged through the outlet (146) while the flue gas is cooled down to 80°C and exits through the outlet (147).
  • the bio-oil is a black liquor comprising 20 to 25% of water, 25 to 30% water insoluble pyro lytic lignin, 5 to 12% organic acids, 5 to 10% non-polar hydrocarbons, 5 to 10%) anhydrosugars and 10 to 25% of other oxygenated compounds.
  • the calorific value of the liquid fuel is typically 16,700 to 18,000 kJ/kg.
  • the biomass feedstock being carried along by the vortex, is heated up rapidly by the hot sidewalls (102b, 106b) at a rate of ⁇ 103K/s to ⁇ 900°C to set off the gasification process.
  • the fine particles biomass feedstock are rapidly pyrolyzed, combusted and gasified whereas the coarser or unconverted particulates are carried along by the high speed vortex to swirl upwards in the outer cyclone (101b) and reverse in direction upon reaching the tapered top (104) to swirl down into the inner cyclone (105) through the open top (107).
  • the vortex swirls upwards again upon reaching the tapered section of the inner cyclone (105) and finally exits through the outlet pipe (108) as producer gas.
  • the ash and char is separated out from the vortex flow and discharged through the second opening (109) to the rotary valve feeder (114) and water-cooled discharging screw conveyor (115) to the collection chamber (116).
  • the producer gas is drawn into the cyclone dust collector (142) to separate out the fine particulates and discharge through outlet (143).
  • the cleaned producer gas exits through the outlet (144) and enters the cooler/condenser (145) where excess steam is condensed to water and collected through the outlet (146) and the producer gas is cooled down to 80°C and exits through the outlet (147).
  • the producer gas is composed of 18 to 30% of carbon monoxide, 2 to 7% of hydrogen, 0.2 to 0.9% of methane, 55 to 65% of nitrogen, 0.3 to 1.3% of oxygen and 4 to 14%) of carbon dioxide.
  • the carbon monoxide and hydrogen content can be kept at a consistently high calorific value of 5000 kJ/kg by maintaining the air-to-biomass ratio at an optimum value as well as the temperature at appropriate values.
  • combustion chamber (101a) is required to be used only for heating up purpose at the starting of gasifier and is shut down during normal operation. It should also be noted that no recycle of flue gas from the outlet of cooler/condenser (147) through the branch pipe (148) is necessary when the apparatus is operated as a gasifier.
  • the heat required for the gasification process is supplied by combustion of portion of feedstock inside the reactor chamber to sustain the temperature for gasification up to 950°C.
  • One of the unique features of the embodiment of the patent is enabling longer residence time for a complete conversion process of biomass feeds to the required products.
  • the entrained vortex flow is forced to swirl three times inside the apparatus in opposite directions, increasing the residence time to allow a wider range of acceptable size of biomass feed particles for complete thermal or thermochemical conversion.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Dispersion Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Processing Of Solid Wastes (AREA)
  • Treatment Of Sludge (AREA)

Abstract

La présente invention concerne un appareil permettant de produire des carburants à partir de biomasse, ledit appareil comprenant (i) une chambre de réaction définie par un espace intégral formée par une structure de cyclone inversé externe et une structure de cyclone interne avec une section effilée inférieure à extrémité ouverte et une sortie tubulaire sur le haut. La structure de cyclone interne est enfermée de manière coaxiale à l'intérieur de la structure de cyclone externe; (ii) une chambre de combustion disposé sous la chambre de réaction; de plus, des entrées d'alimentation sont montées de manière tangentielle sur les parois latérales de la structure de cyclone externe et la chambre de combustion pour l'alimentation de biomasse avec le gaz projeté à grande vitesse. La chambre de combustion génère et fournit de la chaleur à la chambre de réaction par combustion de la biomasse jusqu'à des températures de 800 °C. Le stock d'alimentation de biomasse est injecté dans la chambre de réaction pour former un tourbillonnement à grande vitesse, la biomasse étant convertie en produit torréfié, vapeur de carburant ou gaz de gazogène dans des conditions de fonctionnement différentes sous le contrôle d'un PLC. Les produits gazeux sortent à travers la sortie tubulaire en haut tandis que les produits solides ou les résidus solides, tels que la cendre, sont évacués à travers l'ouverture inférieure de la structure de cyclone interne vers un ensemble transporteur à vis sans fin d'évacuation refroidi à l'eau.
PCT/MY2014/050014 2013-12-30 2014-12-15 Appareil permettant de produire des biocarburants à partir de biomasse WO2015102480A2 (fr)

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MYPI2013702567A MY174567A (en) 2013-12-30 2013-12-30 An apparatus for producing biofuels from biomass

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MY159023A (en) * 2011-07-06 2016-11-30 Regenergy Tech Sdn Bhd An apparatus for producing combustible gases from biomass

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