EP4144822A1 - Vergaser und vergasungsreaktor mit mehreren kombinierten reaktionszonen - Google Patents

Vergaser und vergasungsreaktor mit mehreren kombinierten reaktionszonen Download PDF

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Publication number
EP4144822A1
EP4144822A1 EP22193532.3A EP22193532A EP4144822A1 EP 4144822 A1 EP4144822 A1 EP 4144822A1 EP 22193532 A EP22193532 A EP 22193532A EP 4144822 A1 EP4144822 A1 EP 4144822A1
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EP
European Patent Office
Prior art keywords
reaction zone
gasifier
inlet
gasification
gasification reactor
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.)
Pending
Application number
EP22193532.3A
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English (en)
French (fr)
Inventor
Hans Grassmann
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Isomorph SRL
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Isomorph SRL
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Publication of EP4144822A1 publication Critical patent/EP4144822A1/de
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    • 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
    • C10J3/723—Controlling or regulating the gasification process
    • 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
    • C10J3/007—Screw type gasifiers
    • 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
    • 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
    • C10J2300/0959—Oxygen

Definitions

  • the invention relates to a gasifier and a and gasification reactor for converting carbonaceous feedstock material into a product gas, comprising: a container configured to receive a feedstock material, a gasification reactor extending in a longitudinal direction and arranged downstream the container, and a feeding unit for feeding the feedstock material from the container through the gasification reactor in the longitudinal direction.
  • Gasification of biomass which is referred herein as "gasification process" is performed by a number of sub-processes for converting a biomass feedstock into a product gas. These sub-processes include:
  • a limited amount of oxygen provided by a gasification agent is introduced into the reactor to allow some of the organic material to be "burned” to produce carbon dioxide and energy, which drives a second reaction that converts further organic material to hydrogen and additional carbon dioxide.
  • the gasification agent can be either air, pure oxygen or a mixture of several gasification agents.
  • the combustible products of gasification are in particular carbon monoxide (CO) and hydrogen (H 2 ), with only a minor amount of the carbon completely oxidized to carbon dioxide (CO 2 ) and water.
  • CO carbon monoxide
  • H 2 hydrogen
  • the heat released by partial oxidation provides most of the energy needed to break up the chemical bonds in the feedstock material, to drive the other endothermic sub-processes in the gasification reaction, and to increase the temperature of the final gasification products.
  • Biomass feedstock used for the gasification process may comprise a broad range of different kinds of biomaterials, such as forest and agricultural residues, wood or waste from wood and waste from the food industry, algae, etc.
  • the use of different kinds of biomass results in different challenges and solutions for e.g. pretreatment and feeding of the biomass, for operation of the gasifier, and for cleaning of the produced product gas. Since the biomass varies in size distribution (eg, stalks, stems), a bulk density, and a resulting volumetric energy density, an additional mechanical treatment may be necessary, as for example size reduction and compaction of raw biomass is adjusting the feedstock to the requirements of the conversion process regarding size, homogeneity, and physical properties of the fuel.
  • the process described above may also be referred as an autothermal or direct gasification process.
  • the autothermal gasification process during oxidation the volatile products and some of the char react with limited oxygen in the gasification agent to form carbon dioxide (CO2), carbon monoxide (CO), and in doing so provide the heat needed for subsequent pyrolysis and further reactions for gasifying the pyrolysis products.
  • Pyrolysis starts as the feedstock is exposed to rising temperature in the gasifier due to the partial oxidation. Devolatization and breaking of the weaker chemical bonds occurs, releasing volatile gases such as tar vapors, methane, and hydrogen, along with producing a high molecular weight char, which will undergo further reactions for gasifying.
  • the reactions for gasifying the pyrolysis products into product gas include the combustion of the volatile products contained in the pyrolysis products and some of the char, which react with oxygen to form carbon dioxide primarily and small amounts of carbon monoxide, which provides heat for the subsequent reactions.
  • the gasification process further includes the reaction for gasifying char with steam and carbon dioxide to produce carbon monoxide and hydrogen, via the reactions C + H 2 O ⁇ H 2 + CO and C + CO 2 ⁇ 2 CO. Further reactions occur when the formed carbon monoxide and residual water from the organic material react to form methane and excess carbon dioxide. In addition, further reactions occurs more abundantly in reactors that increase the residence time of the reactive gases and organic materials, as well as heat and pressure.
  • the chemical reactions of the gasification process can progress depend to different extends on the gasification conditions, like temperature and pressure, and the feedstock used.
  • Tar is considered as all organics with a molecular weight larger than that of benzene. Tar condensation at lower temperatures can cause clogging or blockage of pipes, filters, catalyst units, or engines. Thus, one of the main problems in improving the industrial viability of biomass gasification process is related to the presence of tar in the product gas.
  • Tar is a quite complex mixture of different condensable hydrocarbons including one and multiple ring aromatics as well as oxygen containing hydrocarbons.
  • the reforming and cracking reactions require high temperatures, above 1200°C, to be efficient due to high activation energies; in most cases, these are greater than 250-350 kJ/mol.
  • the present invention solves the initially mentioned object by suggesting a gasifier according to claim 1.
  • the gasification reactor has a first inlet for supplying a gasification agent comprising oxygen thereby defining a first reaction zone for the gasification process, the first reaction zone having an extension ⁇ x 1 , in the longitudinal direction.
  • the gasification reactor according to the invention further has a downstream second inlet for supplying the gasification agent thereby defining a second reaction zone for the gasification process, wherein the second reaction zone has an extension ⁇ x 2 in the longitudinal direction.
  • the second inlet is arranged at a distance x 1 from the first inlet, which is preferably defined as x 1 ⁇ ⁇ x 1 + ⁇ x 2 2 , such that the first reaction zone at least partly overlaps the second reaction zone.
  • the distance between the inlets is sufficiently small and the inlets are arranged so close that they form a combined reaction zone without a significant decrease of the temperature between the zones.
  • the maximum temperature in the first reaction zone is defined by T 1 and the maximum temperature in the second reaction zone is defined by T 2
  • the distance between the first inlet and the second inlet is chosen, such that the minimum temperature T Min is defined by the formula T Min ⁇ T 1 + T 2 2 , preferably by T Min ⁇ 4 ⁇ T 1 + T 2 5 .
  • the combined reaction zone is characterized by the fact, that the temperature in the combined reaction zone is first increasing and then approximately constant, without showing significant temperature minima. It shall be understood, that the first reaction zone overlaps the second reaction zone in such a manner that the reactions in the first and second reaction zone are not separated from each other but instead advantageously interact and join each other. In other words, different reactions, e.g. oxidation and reduction, cannot be clearly associated to one of the reaction zones but instead occur over a longer distance with a more constant temperature profile.
  • the zone in which oxidation occurs is not separated from the zone, in which pyrolysis occur.
  • none of the reaction zones has the purpose to drive one particular process, like for instance pyrolysis, and vice versa it is not possible to attribute to any of the processes one particular reaction zone. Instead, all sub-processes may run in the first reaction zone and in the second reaction zone.
  • due to the increased residence time further reactions subsequent gasifying char with steam and carbon dioxide to produce carbon monoxide and hydrogen may occur when the formed carbon monoxide and residual water from the organic material react to form methane and excess carbon dioxide that will decrease the formation of tar and increase the efficiency.
  • the second reaction zone makes use of the increased temperature within the gasification reactor provided by the first reaction zone.
  • the temperature of the feedstock material entering the second reaction zone is higher when compared to the feedstock material entering the first reaction zone. Since, the feedstock material entering of the second reaction zone is pre-heated, the feedstock material can be faster heated to the desired temperature, e.g. T Max or even higher and hold at close to the desired temperature at a longer period.
  • the thermal energy in the gasification reactor is increased due to the holding time without significantly increasing the temperature.
  • the quality of the product gas is improved and subsequent cleaning processes may be reduced or even avoided.
  • the power of the gasifier is increased. This is reasoned by the fact, that the amount of feedstock material that can be converted is not limit to the extension of a single reaction zone, in which the temperature may be sufficiently high for the gasifying the pyrolysis products including e.g. the reaction of the subsequently formed carbon monoxide or carbon dioxide with residual water. It will be understood, that by having two reaction zones the velocity of the feedstock material is not only doubled and instead even higher. This is reasoned by the enlarged zone in which the temperature can be hold sufficiently high for the different sub-processes of the gasification process.
  • overlapping in the context of the invention means, that the temperature which results by the introduction of the gasification agent by the first inlet will not fall significantly, in particular not to the temperature at the very beginning of the gasification reactor, but instead increase again due to the introduction of the gasification agent introduced by the second inlet.
  • the temperature remains above a minimum temperature T Min that is defined by the formula T Min ⁇ T 1 + T 2 2 , preferably by T Min ⁇ 4 ⁇ T 1 + T 2 5 .
  • T Min ⁇ T 1 + T 2 2 preferably by T Min ⁇ 4 ⁇ T 1 + T 2 5 .
  • the temperature between the overlapping reaction zones will not fall at all. Further, not only the temperatures somehow overlap each other, but also the reactions or sub-processes occurring in the reaction zone.
  • a set of inlets arranged at a defined position along the longitudinal axis which is configured for supplying the gasification agent in different radial directions, can also provide the inlet according to the invention.
  • the set of inlets can comprise any number of inlets depending on the size of the gasification reactor. The number of inlets is preferably distributed in a circumferential direction and in particular uniform distributed.
  • the extension of the gasification reactor in the longitudinal direction is preferably larger than the extension in the perpendicular directions.
  • the gasification reactor is configured for partial oxidation of the feedstock material in the first and second reaction zone under supply of the gasification agent to provide a heat amount and for pyrolysis of the feedstock material under supply of said heat amount.
  • the pyrolysis efficiency is increased by directly participating from the heat amount resulting from the oxidation process.
  • the remaining feedstock material that has not been converted into the pyrolysis product can react with the oxygen in the gasification agent to maintain the required heat.
  • the gasification reactor further has a number i of inlets downstream the first inlet and the second inlet for supplying gasification agent, thereby defining a number i of reaction zones each having an extension ⁇ x i in the longitudinal direction, wherein starting from the second inlet each inlet is arranged at a distance x i in the longitudinal direction from the respective upstream adjacent inlet, which is preferably defined as x i ⁇ ⁇ x i ⁇ 1 + ⁇ x i 2 .
  • each reaction zone at least partly overlaps the upstream adjacent reaction zone.
  • the temperature in the gasification reactor is first increasing and then approximately constant, without significant temperature minima.
  • the multitude of zones serves for the creation of one large reaction zone with an even temperature profile.
  • the inlets are uniform distributed in the in the longitudinal direction having an equal distances x i from the respective upstream adjacent reaction zone.
  • the distance between the inlets required to hold the temperature in the subsequent reaction zones in a desired temperature range is simple to calculate.
  • the gasification reactor is configured for pyrolysis of the feedstock material in the reaction zone at a temperature between 300°C and 600°C to form a pyrolysis product and for gasifying the pyrolysis product in the reaction zone at a temperature between 700°C and 1500°C to form a product gas.
  • the pyrolysis products react further at relatively high temperatures between 700°C and 1500°C with the gasification agent or product gases by numerous chemical reactions as described above.
  • the gasification reactor configured for pyrolysis of the feedstock material in the reaction zone at a temperature between 300°C and 600°C is adapted to withstand that temperatures by an appropriate choice of materials and joining processes.
  • the container and/or the gasification reactor is configured for heating the feedstock material up to an evaporation temperature above 100°C to evaporate water contained in the feedstock material.
  • the gasification reactor is preferably equipped wit a heater for heating the feedstock material up to an evaporation temperature above 100°C.
  • the gasification reactor has a frustoconical end portion, in particular arranged in an area downstream the feeding unit.
  • At least one inlet is defined by a first inlet and a second inlet arranged opposite the first inlet.
  • the gasification agent is introduced more uniform into the gasification reactor.
  • At least the first inlet has the form of a slit, wherein the slit preferably extends perpendicular to the longitudinal direction.
  • the first inlet arranged subsequently downstream of the container, may be obstructed by the feedstock material and ash from partial oxidation. By having at least one inlet formed as a slit, the obstructions are reduced.
  • the gasification reactor has a supply for the gasification agent, and the gasifier further has a control unit being in signal communication with the supply for controlling the amount of gasification agent provided by the supply at least to the first and second inlet.
  • the supply of the gasification agent may be selectively controlled thereby in accordance with the feedstock material or other process conditions. It will be understood, that the supply is directly or indirectly in fluid connection with each of the inlets.
  • the gasification reactor has at least one detection unit configured to detect a temperature and/or a pressure at least at one of the inlets and/or in at least one of the reaction zones.
  • the control unit may control the supply in accordance with the detected temperature and/or pressure to reach a predefined temperature or pressure.
  • the gasification reactor has a shell enclosing the at least one inlet, which is in fluid communication with the supply for the gasification agent.
  • the supply is indirectly in fluid communication with the inlets via the shell.
  • the shell provides a uniform pressure control of the inlets and a uniform pressure supply. Further, the shell protects the inlets from dirt and dust from the environment.
  • the gasification reactor has a cleaning mechanism for automatically cleaning at least the first inlet without interrupting gasifier.
  • the cleaning mechanism may comprise a nozzle in fluid communication with the supply for cleaning the inlet by means of pressurized air.
  • the invention relates in a first aspect to a gasifier.
  • the invention in a second aspect, relates to a gasification reactor for gasification of a feedstock material in a gasifier, in particular in a gasifier according to the first aspect of the invention.
  • the gasification reactor according to the second aspect extends in a longitudinal direction and is configured to be arranged downstream a container of the gasifier and to cooperate with a feeding unit for feeding the feedstock material from the container through the gasification reactor in the longitudinal direction.
  • the gasification reactor solves the initially mentioned object by a first inlet for supplying a gasification agent comprising oxygen, thereby defining a first reaction zone, which has an extension ⁇ x 1 , in the longitudinal direction, and in that the gasification reactor further has a downstream second inlet for supplying the gasification agent thereby defining a second reaction zone.
  • the second reaction zone has an extension ⁇ x 2 in the longitudinal direction and is arranged at a distance from the first inlet, which is preferably defined as x 1 ⁇ ⁇ x 1 + ⁇ x 2 2 , such that the first reaction zone at least partly overlaps the second reaction zone. In the first and/or second reaction zone all sub-processes of the gasification process may occur.
  • the gasification reactor according to the second aspect of the invention may be used in a gasifier according to the first aspect of the invention.
  • Preferred embodiments and benefits according to the first aspect of the invention are therefore also preferred embodiments and benefits of the gasification reactor according to the second aspect and vice versa.
  • the invention in a third aspect, relates to a power generation system, comprising a functional unit configured to provide a thermal and/or an electric energy by combustion of a product gas, and a gasifier according to the first aspect of the invention, which is in fluid communication with the functional unit.
  • the gasification reactor or a number of gasification reactors may be configured to provide the product gas for operating the functional unit.
  • the gasification reactor may be configured to provide the product gas for operating a number of functional units.
  • the power generation system according to the third aspect of the invention having a gasifier according to the first aspect of the invention makes use of the benefits described above with respect to the first aspect of the invention. Therefore, preferred embodiments and benefits according to the first aspect of the invention are therefore also preferred embodiments and benefits of the power generation system according to the third aspect and vice versa.
  • the functional unit comprises an electric generator for conversion of kinetic energy into electrical energy and a combustion engine configured to advance the supply kinetic energy to the generator, wherein the gasifier is configured to provide the product gas for operating the combustion engine.
  • the invention relates to a method for operating a gasifier, in particular a gasifier according to the first aspect of the invention, comprising the steps:
  • the method for operating a gasifier makes use of the benefits described above with respect to the gasifier according to the first aspect by defining a first and a second reaction zone due to the introduction of the gasification agent. Therefore, preferred embodiments and benefits according to the first aspect of the invention are therefore also preferred embodiments and benefits of the power generation system according to the fourth aspect and vice versa.
  • the temperature varies along each extension ⁇ x i of the respective reaction zone. It is preferred, that the distances x i of the inlets is chosen such that the temperature first increases in the direction of the material flow, which is the longitudinal direction, and remains above a minimum temperature T Min that is defined by the formula T Min ⁇ T i ⁇ 1 + T i 2 , preferably by T Min ⁇ 4 ⁇ T i ⁇ 1 + T i 5 .
  • the temperature may fall below said minimum temperature, since there is no overlapping area of the reaction zones provided.
  • Fig. 1 shows a gasification reactor 1 according to the prior art.
  • the gasification reactor 1 comprises a pipe 3 defining a flow path for a feedstock material.
  • the gasification reactor 1 further has an inlet, which is defined as a set of inlets 7, 8 arranged in the pipe 3 and distributed in the circumferential direction.
  • an inlet which is defined as a set of inlets 7, 8 arranged in the pipe 3 and distributed in the circumferential direction.
  • only two inlets 7, 8 of the set of inlets are indicated by reference signs. It will be understood, that any number of inlets may form the set of inlets.
  • the set of inlets 7, 8 are configured for supplying a gasification agent comprising oxygen.
  • a gasification agent may for example be ambient air.
  • the first inlet 7 and the second inlet 8 define a first reaction zone 5, which has an extension ⁇ x in the longitudinal direction L.
  • the reaction zone 5 starts at a position upstream the set of inlets 7, 8 and extends downstream the set of inlets 7, 8. If the temperature in the reaction zone 5 is sufficiently high a product gas is produced from feedstock material.
  • the feedstock material moves through the pipe 3, wherein the gasification agent supplied by the set of inlets 7, 8 increases the temperature of the feedstock material, such that volatiles, in particular tar droplets, are dissipated from the feedstock material.
  • the gasification agent supplied by the set of inlets 7, 8 increases the temperature of the feedstock material, such that volatiles, in particular tar droplets, are dissipated from the feedstock material.
  • Carbon atoms from the tar droplets as well as the remaining carbon skeleton undergo an oxidation process with the oxygen contained in the gasification agent thereby producing CO 2 .
  • the oxidation process can also be described as a combustion process, since high temperatures are achieved allowing the further sub-processes of the gasification process to convert the remaining pyrolysis and oxidation products into a product gas.
  • the temperature T in the reaction zone 5 is not uniform and instead increases to a maximum T Max proximate downstream the set of inlets 7, 8 and decreases afterwards. In a certain area, the temperature reaches a maximum for the gasification reactions. Upstream and downstream from the reaction zone 5, the feedstock material cannot be converted into a product gas, since the required temperatures are not reached within the gasification reactor 1.
  • the temperature might increase and to some extend also the size of the reaction zone 5, however, the temperature cannot exceed a certain limit without either damaging the walls of the gasifier 10, or requiring expensive technical measures, like ceramic insulations.
  • the gasification reactor 1 converts the feedstock material completely into a product gas within the reaction zone 5, the feedstock material moves at a velocity sufficiently low such that the feedstock material may be converted along the extension ⁇ x under the given flow of gasification agent.
  • the amount of gasification agent supplied to the gasification reactor 1 may be increased.
  • the conversion of the feedstock material is limited by the length ⁇ x of the reaction zone 5.
  • increasing the power will require to increase the temperature within the gasification reactor 1 that may result in damage of the pipe 3.
  • Fig. 2 depicts a gasification reactor 1 according to a first preferred embodiment of the present invention.
  • the gasification reactor 1 extends in a longitudinal direction L and may comprise a pipe 3. Instead of a pipe, any other suitable form can be chosen which allows the transportation of a feedstock material through the gasification reactor 1.
  • the gasification reactor 1 has a first set of inlets 7.1, 8.1 arranged opposite to each other, which define a first inlet for supplying a gasification agent comprising oxygen to the gasification reactor 1.
  • a gasification agent comprising oxygen
  • the number of inlets may form the set of inlets.
  • the number of inlets may be uniform distributed in the circumferential direction providing a more uniform supply of the gasification agent at a predefined position in the longitudinal direction L.
  • the first set of inlets 7.1, 8.1 define a first reaction zone 5.1.
  • the first reaction zone 5.1 has an extension ⁇ x 1 , in the longitudinal direction L.
  • the gasification reactor 1 further has a second inlet defied by a second set of inlets 7.2, 8.2 arranged opposite to each other.
  • the second set of inlets 7.2, 8.2 is arranged downstream the first set of inlets 7.1, 8.1 at a distance x 1 in the longitudinal direction L.
  • only two inlets 7.2, 8.2 of included in the set of inlets are indicated by reference signs. It will be understood, that any number of inlets may form the set of inlets.
  • the number of inlets may be uniform distributed in the circumferential direction providing a more uniform supply of the gasification agent at a predefined position in the longitudinal direction L.
  • the second set of inlets 7.2, 8.2 define a second reaction zone 5.2.
  • the second reaction zone 5.2 has an extension ⁇ x 2 in the longitudinal direction L.
  • Fig. 2 thereby illustrates the size and the temperature of this reaction zone 5.1 as it would be in the absence of the downstream inlets 7.2, 8.2.
  • zone 5.2 is shown, as it would be in absence of the upstream inlets 7.1, 8.1.
  • the distance x 1 is smaller than the extension ⁇ x 1 , of the first reaction zone and the extension ⁇ x 2 of the second reaction zone.
  • an overlapping area 9.1 in which the first reaction zone 5.1 overlaps the second reaction zone 5.2 is provided.
  • reaction zones 5.1 and 5.2 as shown in Fig. 2 are illustrated, as they would result in the absence of any neighboring inlets. If instead the gasification agent is supplied to all inlets, the temperatures profiles of reaction zones 5.1 and 5.2 will in first approximation add to a common reaction zone. As a result, the maximum temperature T Max is not reached in only the maxima of 5.1 and 5.2, but rather over the whole length of x 1 . Therefore, the volume within the gasification reactor 1 in which high-temperature reactions can occur, strongly increases.
  • the velocity of the feedstock material through the gasification reactor 1 is limited by the time needed to convert the whole feedstock material arranged along a predefined extension (not shown) within the respective reaction zone.
  • the velocity of the feedstock material through the gasification reactor 1 can be increased and thus resulting in an increased power of the gasification reactor 1.
  • twice of the amount of feedstock material can be converted into a product gas within the same time due to the first reaction zone 5.1 and the second reaction zone 5.2. Since the amount of gasification agent supplied to each one of the reaction zones 5.1, 5.2 remains constant when compared to the gasification reactor 1 shown in Fig. 1 , the temperature will not be increased and thus damage of the pipe 3 can be avoided.
  • the gasification reactor 1 has a first set of inlets 7.1, 8.1 defining a first reaction zone 5.1.
  • the gasification reactor 1 further has a second set of inlets 7.2, 8.2 defining a second reaction zone 5.2, a third set of inlets 7.3, 8.3 defining a third reaction zone 5.3 and a fourth set of inlets 7.4, 8.4 defining a fourth reaction zone 5.4.
  • Each one of the sets of inlets 7.1, 8.1, 7.2, 8.2, 7.3, 8.3, 7.4, 8.4 is configured to supply a gasification agent comprising oxygen to the gasification reactor 1.
  • a gasification agent comprising oxygen
  • only two inlets of each set of inlets are indicated by reference signs. It will be understood, that any number of inlets may form the respective set of inlets. The number of inlets may be uniform distributed in the circumferential direction providing a more uniform supply of the gasification agent.
  • the first set of inlets 7.1, 8.1 is arranged at a distance from the downstream second set of inlets 7.2, 8.2.
  • the second set of inlets 7.2, 8.2 is arranged at a distance x 2 from the downstream third set of inlets 7.3, 8.3.
  • the third set of inlets 7.3, 8.3 is arranged at a distance x 3 from the downstream fourth set of inlets 7.4, 8.4.
  • Fig. 3 only the distances x 2 , x 3 are indicated by reference signs by way of example.
  • the distance x 3 is smallerthan the average of the extension ⁇ x 3 of the third reaction zone 5.3 and the extension ⁇ x 4 of the fourth reaction 5.4 zone.
  • an overlapping area 9.3 in which the third reaction zone 5.3 overlaps the fourth reaction zone 5.4 is provided.
  • the inlets can either be uniform distributed over having a varying distance from each other.
  • the first reaction zone 5.1 and the second reaction zone 5.2 overlap each other in an overlapping area 9.1.
  • the third reaction zone 5.3 and the second reaction zone 5.2 overlap each other in an overlapping area 9.2.
  • the fourth reaction zone 5.4 and the third reaction zone 5.3 overlap each other in a third overlapping area 9.3, since the distance between each set of inlets 7.1 - 8.4 and the respective upstream set of inlets is smaller than the associated reaction zone 5.1 - 5.4.
  • the extension in the longitudinal direction L in which the temperature can be held close to the temperature T Max is further increased, and also the power is increased with respect to the situation and in particular the temperature profile described with respect to Fig. 2 .
  • additional inlets may be added, to further increase the length of the high temperature zone and to further increase the power of the gasifier 10.
  • a very compact gasifier 10 with a very high power results, delivering a product gas of high quality.
  • Fig. 4 shows the gasifier 10 according to a first preferred embodiment.
  • the gasifier 10 comprises the gasification reactor 1, a container 11 configured to receive feedstock material.
  • the container 11 is arranged upstream the gasification reactor 1.
  • the gasifier 10 preferably further comprises a feeding unit 13, which is at least partly arranged in the gasification reactor 1, in particular in a pipe 3 of the gasification reactor 1.
  • the feeding unit 13 may be provided by a snake conveyor, which is configured for feeding the feedstock material from the container 11 through the pipe 3 of the gasification reactor 1.
  • the gasification reactor 1 has a number of reaction zones 5.1, 5.2, 5.i defined by a number of inlets i each defined by a set of inlets 7.1, 8.1, 7.2, 8.2, 7.i, 8.i which are configured for supplying a gasification agent to the gasification reactor 1.
  • the feeding unit 13 is preferably arranged upstream the number of reaction zones 5.1, 5.2, 5.i.
  • reaction zones 5.1, 5.2, 5.i are indicated by reference signs. It will be understood, that the number of reaction zones is not limited to the number shown in the embodiment.
  • Fig. 5 shows the gasifier 10 according to a second preferred embodiment.
  • the embodiment shown in Fig. 5 differs from the embodiment shown in Fig. 4 by the form of the gasification reactor 1.
  • the gasification reactor 1 in Fig. 5 has a frustoconical end portion 14 arranged in an area downstream the feeding unit 13 such that the cross section of the gasification reactor 1 increases with the distance from the feeding unit 13 in the longitudinal direction L.
  • the feedstock material is transported from a lower end of the gasification reactor 1 to its upper end.
  • the frustoconical end portion 14 allows the supply of the gasification agent with an increased velocity, since the weight force provided by the feedstock material within the end portion 14 avoids the acceleration of the product gas and/or oxygen to an extent which results in an undesired moving away of the remaining feedstock material.
  • Fig. 6 shows the gasifier 10 according to a third preferred embodiment.
  • the gasifier 10 shown in Fig. 6 differs from the gasifier shown in Fig. 4 , on the one hand, by a shell 15 that encloses the sets inlets 7.1, 7.2 - 7.i, 8.i defining a number of reaction zones 5.1 - 5.i.
  • the shell 15 provides a gasification agent supplied by a supply 17 access to the each one of the sets of inlets 7.1, 7.2 - 7.i, 8.i.
  • the shell 15 is coaxially arranged to the gasification reactor 1 at a distance in the radial direction, such that the gasification agent can be well distributed before entering the sets of inlets 7.1, 7.2 - 7.i, 8.i.
  • the gasifier 1 hat control unit 19 being in signal communication with the supply 17.
  • the control unit 19 is configured to control the amount of the gasification agent supplied by the supply 17 to the number of inlets 7.1, 7.2 - 7.i, 8.i.
  • the gasifier may further has a detection unit 21, which is in signal communication with the control unit 19.
  • the control unit 19 may selectively control the supply 17 for supplying an amount of the gasification agent to a respective one of the number of fluid inlets 7.1, 7.2 - 7.i, 8.i based on a signal provided by the detection unit 21.
  • the detection unit 21 is preferably arranged within the shell 15.
  • the detection unit 21 may comprise a temperature sensor or a pressure sensor for detecting the temperatures within a respective one of the reaction zones 5.1 - 5.i or the pressures at a respective one of the inlets 7.1, 7.2 - 7.i, 8.i.
  • control unit 19 may selectively increase the amount of gasification agent supplied by the supply 17 to a predefined one of the fluid inlets 7.1, 7.2 - 7.i, 8.i to increase the temperature and/or pressure.
  • Fig. 7 depicts a power generation system 100 according to a first preferred embodiment.
  • the power generation system 100 may comprise a functional unit 23 configured to provide a thermal and/or an electric energy by the combustion of a product gas.
  • the power generation system 100 further comprises a gasifier 10 according to a preferred embodiment of the invention.
  • the gasifier 10 comprises a container 11, a gasification reactor 1 arranged downstream the container 11, and a feeding unit 13 configured for feeding a feedstock material from the container 11 through the gasification reactor 1.
  • the power generation system 100 further comprises a conduit 25 for supplying the product gas from the gasifier 10 to the functional unit 23.
  • the gasifier 10 is configured for converting the feedstock material received in the container 11 into a product gas in the at least two reaction zones as described with regard to Figs. 2 and 3 .
  • the functional unit 23 may be a thermal power plant, a chemistry plant configured for converting the product gas into a fuel, or a vehicle, which is advanced by combustion of the product gas.
  • Fig. 8 shows a second preferred embodiment of the power generation system 100.
  • the functional element is a combustor 27 configured to combust the product gas provided by the gasifier 10 in order to provide thermal energy.
  • Said thermal energy may be provided to a district heating pipeline used for heating any kinds of buildings or plants.
  • Fig. 9 shows a power generation system 100 according to a third preferred embodiment.
  • the power generation system 100 comprises a gasifier 10 as described with respect to Figs. 4 to 6 .
  • the functional unit in this embodiment is provided by a combustion engine 31 and an electric generator 29.
  • the electric generator 29 is configured to convert kinetic energy into electric energy.
  • the gasifier 10 converts a biomass feedstock material, which is received in the container 11 into a product gas by a gasification process.
  • the product gas is used to operate a combustion engine 31, as, for example, a combustion motor.
  • the combustion engine 31 is configured to provide kinetic energy by combusting a fuel as, for example, the product gas.
  • the generator 29 then converts the kinetic energy provided by the combustion engine 31 into electric energy in a known manner.
  • the amount of product gas provided to the combustion engine 31 or to the functional unit 23 shown in Fig. 7 orto the combustor 27 shown in Fig. 8 depends on the amount of feeding material that can be converted into product gas in a predefined time frame.
  • the power of the power generation system 100 depends on the velocity in which the feedstock material can move through the gasification reactor 1 allowing a total conversion of the feedstock material.
  • the conversion rate depends on the temperature, which is limited by possible damage of the gasification reactor 1 as described above.
  • the gasifiers shown in Figs. 4 to 6 may be operated by a method comprising the feeding of a feedstock material from the container 11 through the gasification reactor 1 in the longitudinal direction L.
  • the method further comprises supplying a gasification agent to the first reaction zone 5.1 and the second reaction zone 5.2 via the corresponding first set of inlets and via the second set of inlets 7.2, 8.2.
  • the gasification agent may be supplied to a number of downstream-arranged subsequent reaction zones via their corresponding inlets.
  • the method further includes partially oxidizing the feedstock material under supply of the gasification agent in at least one of the reaction zones to provide a heat amount for the subsequent pyrolysis of the feedstock material in said reaction zones to provide a pyrolysis product.
  • the method includes finally gasifying the pyrolysis product, preferably in the absence of oxygen, into a product gas. Since the amount of feedstock material will decrease in the downstream direction and the amount converted into pyrolysis products and product gas and the amount consumed in oxidation will increase, at some point combustion and reduction reactions may increase compared to the pyrolysis reactions mainly occurring in the reaction zones subsequent the feeding unit 13.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
EP22193532.3A 2021-09-01 2022-09-01 Vergaser und vergasungsreaktor mit mehreren kombinierten reaktionszonen Pending EP4144822A1 (de)

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1996032163A1 (en) * 1995-04-11 1996-10-17 Moraski Dennis P Biomass solids gasification system and process
WO2013068052A1 (en) * 2011-11-09 2013-05-16 Siemens Aktiengesellschaft Method and system for producing a producer gas
US20140283453A1 (en) * 2013-03-19 2014-09-25 Robert Clark Tyer, SR. Tyer carburetion process
DE102016121046A1 (de) * 2016-11-04 2018-05-09 HS TechTransfer UG (haftungsbeschränkt) & Co. KG Duplex-TEK-Mehrstufen-Vergaser

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1996032163A1 (en) * 1995-04-11 1996-10-17 Moraski Dennis P Biomass solids gasification system and process
WO2013068052A1 (en) * 2011-11-09 2013-05-16 Siemens Aktiengesellschaft Method and system for producing a producer gas
US20140283453A1 (en) * 2013-03-19 2014-09-25 Robert Clark Tyer, SR. Tyer carburetion process
DE102016121046A1 (de) * 2016-11-04 2018-05-09 HS TechTransfer UG (haftungsbeschränkt) & Co. KG Duplex-TEK-Mehrstufen-Vergaser

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