Classifications

• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
  • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
  • C10J3/60—Processes
  • C10J3/64—Processes with decomposition of the distillation products
  • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
  • C10J3/02—Fixed-bed gasification of lump fuel
  • C10J3/20—Apparatus; Plants
  • C10J3/32—Devices for distributing fuel evenly over the bed or for stirring up the fuel bed
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
  • C10J3/02—Fixed-bed gasification of lump fuel
  • C10J3/20—Apparatus; Plants
  • C10J3/34—Grates; Mechanical ash-removing devices
  • C10J3/40—Movable grates
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
  • C10J3/72—Other features
  • C10J3/74—Construction of shells or jackets
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
  • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
  • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
  • C10K3/003—Reducing the tar content
  • C10K3/008—Reducing the tar content by cracking
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2200/00—Details of gasification apparatus
  • C10J2200/15—Details of feeding means
  • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2300/00—Details of gasification processes
  • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
  • C10J2300/0953—Gasifying agents
  • C10J2300/0956—Air or oxygen enriched air
• • 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
  • Y02E20/00—Combustion technologies with mitigation potential
  • Y02E20/14—Combined heat and power generation [CHP]
• • 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
  • Y02P20/10—Process efficiency
  • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

• the invention relates to a device for the multi-stage gasification of carbonaceous fuels, namely biomass, for the production of generator gas in cogeneration plants with a low content of tar and other impurities.
• Biomass is considered to be a carbon-based material of plant or animal origin and a renewable source of energy.
• woody biomass obtained by processing tree and shrub vegetation into the form of wood chips, sawdust, briquettes, pellets, etc.
• Energy is extracted from plant biomass by thermal or biochemical processes, while the thermal processes include liquefaction, pyrolysis, gasification, and combustion.
• Gasification is a partial oxidation process where the biomass is first burned, then the resulting flue gases are introduced to uncombusted and pyrolytically decomposed fuel, resulting in the chemical conversion of the flue gas to producer gas.
• Producer gas is a mixture of combustible carbon monoxide, hydrogen, tars, and lesser amounts of carbon dioxide, methane and other components.
• gasifier devices for smaller heat capacities from 0.5 Wt to 2 MWt with a fixed bed which, according to the methods used to direct the flow of fuel and gas, may be divided into countercurrent and concurrent flows.
• the advantage of countercurrent gasifier devices is that they have very good thermal efficiency, have minimal mechanical unburned residues, and are of simple construction, thus also representing lower investment costs.
• the disadvantages of the countercurrent gasifier device consist in the fact that the product gas is polluted by tar in the hundreds of g/m 3 and, through expensive and complicated methods, must be cleaned to the pollution level permitted for the production of electrical energy in gas cogeneration units, which is maximally 20 mg/m 3 .
• the cocurrent gasifier device can produce relatively clean product gas; with a heat output of a gasifier device above 0.5 Wt, however, the tar content in the product gas rapidly increases, resulting in the repeated necessity of expensively cleaning the tar from the product gas.
• the greatest disadvantage of these gasifier devices is the need to use fuel in coarser granulometry with a small proportion of fine fractions, otherwise the gasification process is uneven with large fluctuations in pressure losses.
• Such multi-stage gasifier devices may include the subject of the invention according to patent CZ 295171 , which describes a three-zone biomass gasifier device.
• the three-zone biomass gasifier device consists of a vertically oriented construction consisting of mutually-nested inserted cylindrical containers which delimit individual zones within the gasifier device, wherein a biomass dispenser opens from above into the highest container while a revolving bed is arranged at the bottom of the lowest container.
• the containers have different diameters, with the highest container having the smallest diameter.
• the bed is designed as a horizontal rotating table top, which is equipped in its center with a perforated conical grate through which the gasifying medium flows into the container.
• a tray to catch the ash is arranged under the table.
• the disadvantages of the three-zone gasifier device consist in the fact that the biomass is processed unevenly, it must be pre-dried, and that the gasifier device is structurally demanding with high investment costs because it uses a moving bed, which is stressed and subject to faulting from the dimensional dilation due to high temperatures; furthermore the device is problematic in its discharge of product gas and capture of return gas which is achieved by testing and specific setting, as shown in the example of its execution.
• the gasifier device according to the invention has no pyrolysis area, and it also has insufficiently effective separation of individual work zones, since the combustion zone and reduction zone are mostly in the same space, and it is known for its poor controllability and flexibility of performance.
• the task of the invention is to create a device for the multi-stage gasification of carbonaceous fuels with a very low tar content in the product gas, and which would be structurally simple, have a sufficient area for pyrolysis, a high conversion efficiency of the reduction zone, would process a large range of fuels with different granulometry, would have a well-controllable performance, would permit easy sizing of the device according to the required performance, and would provide a long service life while achieving low operating and maintenance costs.
• the device for multi-stage gasification of carbonaceous fuel includes a hermetically sealed vertical container with a pyrolysis chamber, wherein the container is insulated and is adapted for filling the container with carbonaceous fuel from the top of the container and for removing ash from the bottom of the container.
• the device further includes a partial oxidation chamber for the oxidation of the pyrolysis products enclosed in a refractory casing which is essentially defined by a conical, cylinder, or pyramid shape, and which is equipped with oblique air passages.
• the device also contains a reduction zone for the chemical reduction of oxidized product gas released from the partial oxidation chamber, wherein at least one secondary air inlet leads into the chamber and at least one outlet for product gas leads out of the vessel.
• the subject-matter of the invention consists in the fact that the reduction zone is arranged beneath the casing of the partial oxidation chamber inside the container, formed by a retarder for slowing the progression of carbonized pyrolysis residue of fuel through the container vertically oriented towards the reduction zone, wherein the product gas outlet is arranged beyond the reduction zone in the direction of the process of the product gas out of the device.
• the casing of the partial oxidation chamber delimits a f ree space for the progress of oxidation of the volatile constituents, the fuel including the tars, in the partial oxidation chamber, since the pyrolysis residue of the fuel does not accumulate in the partial oxidation chamber where it would obstruct, but leads down the casing into the reduction zone.
• the advantage is that the product gas is forced to leave the container of the device by passing through the reduction zone where, thanks to suitable chemical physical conditions, the reduction of incombustible CO 2 to combustible CO may occur, thereby increasing the heat potential of the product gas for the cogeneration unit.
• the pyrolysis chamber is formed by at least one vertically oriented pyrolysis channel for the passage of fuel into the partial oxidation chamber, separate from the container, and between the pyrolysis channel and the container there is a space for passage of the product gas from the bottom part of the container into the upper part of the container by bypassing the pyrolysis channel into the outlet for product gas arranged in the upper part of the container.
• the pyrolysis channel forms a heat transfer surface thus allowing for the exchange of heat, wherein the heat from the product gas is transferred to the fuel stored in the pyrolysis channel, wherein the heat causes a pyro!ytic decomposition of the fuel before the leaving the pyrolysis channel and the subsequent passage of fuel to the pyrolysis chamber.
• an integral lining arranged which forms, in the upper part of the container, a hopper opening into a set of vertical pyrolysis channels which are arranged separately from each other and from the container, and which lead together to the central part of the integral lining forming an interspace and a partial oxidation chamber with a refractory casing, and a lower portion of the integral lining forms a reduction zone, wherein between the outer casing of the integral lining and the inner wall of the container there is a space for the passage of the product gas from the reduction zone by bypassing the integral lining to the outlet.
• the integral lining delimits the individual active areas within the container and allows for the flow of product gas in the space between the container wall and the lining wall, thereby providing conditions for the efficient transfer of heat to the fuel in the pyrolysis channels.
• the integral lining includes nozzles of primary air, for an easy start and regulation of the device's power, connected to the inlet of primary air passing through the casing of the container and casing of the integral lining.
• the nozzles of the primary air the support pyrolytic decomposition of the fuel, while the temperature inside the device slowly increases, which affects the function and performance of the device.
• the speed of pyrolytic decomposition of fuel, the temperature in the device, and the quantity of gaseous substances produced all change.
• the nozzles are radially arranged to line the inner circumference of the integral liner. If the air jets would not bring air around the entire perimeter of the integral liner, this would result in the formation of one pyrolysis focal point of fuel in the interspace of the integral liner, and the fuel would be distributed unevenly, and the non-distributed fuel would clog the reduction zone and have a negative impact on the operation of the equipment.
• the integral liner inside has at least one support that bears a refractory casing, wherein through the support there passes, through the casing of the container and through the casing of the integral lining, an inlet for secondary air which leads to nozzles of secondary air arranged below the refractory casing.
• the partial oxidation chamber there must be, for the course of the oxidation, a sufficient amount of oxygen, which is fed into the chamber by the secondary air inlet.
• the tar is degraded into simpler compounds in the free space of the partial oxidation chamber.
• a feeder opens to the upper part of the container with airtight stoppers for the supply of fuel and opening up above the hopper, while a mixer is also arranged in the upper part of the container that extends into the hopper.
• the feeder is hermetically sealed in order to prevent the loss of pressure when filling the hopper of the device which would lead to a disruption of the pressure environment within the container of the device. The change in pressure would affect the process of pyrolytic decomposition of the fuel and would have an impact on the device's performance.
• the mixer ensures sufficient fuel distribution to each channel of the set of pyrolysis channels.
• the device for multi-stage gasification of carbonaceous fuels in the bottom part of the container there is a movable grate for shoveling the ash for its removal to the discharge pipe, equipped with an airtight stopper. Even when shoveling the ash, the pressure balance in the device must be maintained to avoid affecting the performance of the device, while the grate evenly shovels the ash from around the entire the bottom of the device.
• the device for multi-stage gasification of carbonaceous fuels there are supports distributed throughout the inner circumference of the integral lining, wherein between the supports there are gaps formed for the gravity fall of the pyrolysis residue of fuel from the surface of the refractory casing into the reduction zone.
• the supports must bear the weight of the refractory casing, which the fuel exerts pressure on, so there must be several of them and they must be strong enough, while at the same time it is necessary that the pyrolysis residue of the fuel can fall into the reduction zone, necessitating the gaps between the supports.
• vents in the refractory casing arranged vertically above one another and are obliquely oriented to prevent the ingress of pyrolysis residues of fuel into the vents. If fuel residues would penetrate into the vents, this would result in plugging or cause an accumulation of residues in the partial oxidation chamber, thereby decreasing its void volume and decreasing the efficiency of the decomposition of tars.
• the integral lining is a steel weldment
• the number of vertical pyrolysis channels is from one to eight
• a cross- section of the vertical pyrolysis channels forms a circle or circular arc.
• the advantages of the device according to the invention consist in a low tar content in the product gas, in the ease of operation of the device's performance, in almost wasteless operation, in a wide range of dimensions of the overall performance of the device, in the use of the heat of the product gas, and in the possibility of using fuels of different granulometry.
• FIG. 1 shows a vertical sectional view of the device
• Fig. 2 shows a horizontal sectional view of the container and integral lining with one pyrolysis channel with a circular cross- section
• Fig. 3 shows a horizontal sectional view of the container and integral lining with four pyrolysis channels with circular arc cross-sections
• Fig. 4 shows a horizontal sectional view of the container and integral lining with four pyrolysis channels with circular cross-sections.
• the device 1 for multi-stage gasification of carbonaceous fuels 2 consists of a vertical cylindrical container 3.
• the container 3 has a cylindrical shape and is made of refractory steel.
• the outer casing of the container 3 is lined with a thermal insulation plate 4 for high temperatures.
• the upper base of the container 3 is basically formed into a conical shape, while on its top a driver is mounted, in a vertical downward direction, for the mixer 16i.
• the carbonaceous fuel 2 consists of wood chips with a moisture content of 10% - 15% while the size of the fraction of fuel 2 is 5 mm to 50 mm.
• the lower base of the container 3 forming the bottom is horizontal and is equipped (not shown in Fig. 1) with a water cooling system for the bottom for cooling the ash 5 as it is being removed.
• a rotary grate 18 with rectangular arms for moving the ash 5 into the outlet pipe 19 with airtight valves for maintaining the pressure conditions inside the container 3.
• an integral lining 14 passes through almost the entire height of the container 3, wherein, between the outer side of the wall of the integral lining 14 and the inner side of the wall of the container 3, a space is created for the product gas 11 , to pass through.
• the integral lining 14 forms a hopper 23 for the fuel 2, in which the mixer 16 moves and into which the feeder 22 for the fuel 2 opens up.
• the hopper 23 extends completely through the cross-section of the container 3.
• the hopper 23 of the integral lining 14 opens in a downward direction through the container 3 into a set of four pyrolysis channels 15 which are formed by pipes and between which there is a free space
• the number of pyrolysis channels 15 and their cross-sections may differ, for example, only three pyrolysis channels 15 with a cross- section in the shape of circular arcs.
• the pyrolysis channels 15 open up into the central part of the integral lining 14, forming an interspace 6.
• a fireclay lining 26 is formed, through which primary air nozzles 17 pass around the entire circumference.
• the primary air inlet 25 passes through the wall of the container 3 and the wall of the integral lining 14.
• the integral lining 14 opens up above the bottom base of the container 3, wherein the fireclay lining 26 is walled along the inner circumference over where it opens; on the fireclay lining 26 there are placed, with sufficient spacing, supports 20 for supporting a conical ceramic casing 8 of the partial oxidizing chamber 7. Throughout these supports 20 and passing into the partial oxidation chamber 7 there are nozzles 24 supplying secondary air from the inlet 12.
• the ceramic casing 8 is equipped with vents 9 oriented obliquely upward so that the pyrolysis residue of the fuel 2 does not fall into the partial oxidation chamber 7.
• the product gas ⁇ ⁇ _ is discharged from the container 3 through outlet 13 in the area above the hopper 23.
• the fuel 2 descends through the heated pyrolysis channels 15, dries, then its gradual pyrolysis occurs through the influence of the transmitted heat.
• the evaporated moisture from the fuel 2 in the form of steam and later the released volatile component sequentially flow through the entire cross- section of each pyrolysis channel 15, the fuel 2 heats up, so the fuel 2 is pyrolyzed at a greater distance from the heat exchange surface of the pyrolysis channel 15, so that upon the exit of fuel 2 from the pyrolysis channels 1J5 into the interspace 6 above the partial oxidation chamber 7, the fuel 2 is spread over the carbon-containing pyrolysis remainder of the fuel 2 and the volatile component.
• the simplest shape of the pyrolysis channel 15 is formed by a pipe.
• An increase in the total pyrolysis heat exchange surface may be achieved, for example, by increasing the total number of pyrolysis channels 15.
• a square shaft with an n-angle section may also serve as a pyrolysis channel 15.
• the pyrolysis residue of the fuel 2 falls freely along the outer contour of the conical casing 8 of the partial oxidizing chamber 7, which is made of refractory ceramic or alloy, and gradually flows into the reduction zone 10 located below the partial oxidizing chamber 7.
• the refractory casing 8 is supported by several (e.g. four) supports 20, between which are wide gaps 2 allowing the pyrolysis residue of the fuel 2 to enter into the reduction zone 10.
• the gaseous component released from the fuel 2 above the partial oxidizing chamber 7 passes through the oblique vents 9 in the cone of the casing 8 into the partial oxidation chamber 7.
• nozzles 24 connected to the secondary air inlet 12 enter tangentially in the bottom part. This is also the most frequent air.
• Partial combustion (oxidation) of the volatile components and of the gas released from the fuel 2 occurs, and the temperature in the partial oxidation chamber 7 increases to 1000-1200° C. This leads to the thermal decomposition of the tars in the volatile components and in the released gas. This is also greatly contributed to by the long time that the released gas remains in the partial oxidation chamber 7, due to its large volume as delimited by the cone of the casing 8.
• the hot gases from the partial oxidation chamber 7 are stripped of residual tars, and their potential calorific value is also increased by reduction of the resulting CO 2 to CO, which is flammable.
• the resulting gas mixture which creates product gas 11_, then freely exits through the space between the casing of the integral liner 14 and casing of the container 3 and further through the space between the pyrolysis channels 15 out of the device through outlet 13 for product gas 1 .
• the product gas 11 transfers heat to the fresh inserted fuel 2 descending through the pyrolysis channels 15.
• the reduction of temperature of the exiting product gas 11. and the use of its heat for the drying out and pyrolysis of the fuel 2 in the pyrolysis channels 15 substantially increases the thermal efficiency of the device 1. It is also important to completely insulate the container 3 with insulation 4 around the outer casing of the container 3.
• a system of nozzles 17 connected with the primary air inlet 25 is used, wherein this system is located around the circumference of the interspace 6 above the conical casing 8 of the partial oxidizing chamber 7.
• the fuel 2 ignites, thereby increasing the temperature in the partial oxidation chamber 7-
• the opening of the inlet 12 of secondary air flowing through the nozzles 24 into the partial oxidation chamber 7 where the temperature begins to rapidly increase After its stabilization to a set temperature between 1000°C - 1200°C and a sufficient heating of the reduction zone 10, the product gas 1 is ready for use in a cogeneration unit.
• the supply of secondary air 12 is regulated so that even during the exchange-related stress to the device 1 , the desired temperature in the partial oxidation chamber 7 is maintained.
• the primary air introduced into the radially formed nozzles 17 around the periphery of the integral body 14 in the lining 26 is regulated so that the vacuum above the fuel 2 in the hopper 23 is maintained in a range from 50 to 100 mbar.
• the area of pyrolysis channels 15 may have different shapes, which, with sufficient dimensioning, allows for the use of fuel with 40% moisture content, thereby saving investment costs designated for the construction of a drying apparatus.
• the casing 8 is fixed to the inner side of the wall of the integral lining 14, and the space delimited by the casing 8 of the partial oxidizing chamber 7 has the shape of an inverted cone oriented with the outlet opening downwards, whereas the partial oxidation chamber 7 itself is located under the casing 8 and, delimited by the cone, the pyrolysis residue of fuel 2 descends towards the interconnecting top of the cone, through which it falls into the reduction zone 10 located below the partial oxidation chamber 7-
• vents 9 or slits for the passage of gas 11. with tar content into the partial oxidation zone 7, into which nozzles 24 open, supplied with secondary air from the inlet 12.
• the device for multi-stage gasification of carbonaceous fuels according to the invention is useful for producing very pure generator gas with a minimal tar content (below 20 mg/m 3 ) for direct use in cogeneration units for the production of electricity and heat with high efficiency.

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• 2013
  • 2013-12-18 CZ CZ2013-28958U patent/CZ26592U1/cs not_active IP Right Cessation
  • 2013-12-19 WO PCT/CZ2013/000173 patent/WO2015090251A1/en active Application Filing

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