Patent Application
20230038042
The invention relates to a pyrolysis system comprising a pyrolysis reactor arranged for producing pyrolysis gas and a first and second condensing unit arranged to cool the pyrolysis gas to condense a first and second pyrolysis liquid. The invention further relates to a method for producing purified pyrolysis gas and pyrolysis liquids and use of a pyrolysis system.
Producing biogas from biomass, coal or other is well known in the art e.g. by means of pyrolysis. However, pyrolysis gas has relatively high content of tar and other unwanted substances and the pyrolysis gas therefore has to undergo some sort of treatment to make it usable.
Thus, from U.S. Pat. No. 9,611,439 B1 it is known to run biomass into a fluid bed pyrolizer to produce pyrolysis gas and then run the pyrolysis gas through a number of condensation stages to condensate different substances and thereby remove them from the pyrolysis gas. However, such a setup is inefficient and difficult to realize.
It is therefore an object of the present invention to provide for a cost-efficient technique for producing purified pyrolysis gas and pyrolysis liquids.
The invention provides for a pyrolysis system comprising a pyrolysis reactor arranged for producing pyrolysis gas and a first condensing unit arranged to cool the pyrolysis gas to a first temperature to condense a first pyrolysis liquid. The system further comprises a second condensing unit arranged to cool the pyrolysis gas to a second temperature to condense a second pyrolysis liquid, wherein the first temperature is higher than the second temperature. The system also comprises a return conduit arranged to guide a portion of the pyrolysis gas back into the pyrolysis reactor to drive the pyrolysis process, and heating means arranged to increase the temperature of the portion of the pyrolysis gas before it reenters the pyrolysis reactor. The pyrolysis reactor is a fixed bed counterflow pyrolysis reactor comprising a pyrolysis gas outlet arranged at an upper part of the pyrolysis reactor through which the produced pyrolysis gas leaves the pyrolysis reactor, a pyrolysis gas inlet arranged at a lower part of the pyrolysis reactor, through which the heated pyrolysis gas reenters the pyrolysis reactor to travel through the feedstock, a feedstock inlet arranged at the upper part of the pyrolysis reactor through which feedstock enters the pyrolysis reactor and a char outlet arranged at the lower part of the pyrolysis reactor, through which char produced in the pyrolysis reactor leaves the pyrolysis reactor.
When producing pyrolysis gas by means of a fixed bed counterflow pyrolysis reactor, the biomass—i.e. the feedstock—is typically introduced from the top and hot gas is typically guided up through the feedstock from the bottom so that the gas is in direct contact with the feedstock during the pyrolysis process. Thus, the produced pyrolysis gas is cooled when traveling up through the colder biomass. In this way the pyrolysis gas is relatively cool when it when it leaves the pyrolysis reactor—typically between 150 to 250 degrees Celsius or even lower. This is advantageous in that the risk of sedimentation or settling of tar and other substances in the pyrolysis gas before these substances are condensed is reduced due to the lower viscosity of these substances at this temperature range. Furthermore, the system also becomes more efficient because less cooling is needed to condensate the substances. And recirculating the pyrolysis gas to drive the pyrolysis process in the pyrolysis reactor is advantageous in that this gas is readily available, it is oxygen-free or has a very low content of oxygen and it is already hot and therefore it does not need to be heated much before it reenters the pyrolysis reactor—all of which ensures a more cost-efficient pyrolysis system.
In this context, the term “fixed bed counterflow pyrolysis reactor” should be understood as any kind of unit capable of running a fixed bed counterflow pyrolysis process. Pyrolysis is a thermochemical decomposition of organic material or fossil fuel at elevated temperatures in the absence of oxygen (or any halogen). Pyrolysis involves the simultaneous change of chemical composition and physical phase and is irreversible. Pyrolysis is a type of thermolyzes and is most commonly observed in organic materials exposed to high temperatures typically starting at 200-300° C. and up to 500 C or even higher. In general, pyrolysis of organic substances or fossil fuels produces gas and liquid products and leaves a solid residue richer in carbon content, which in this embodiment is referred to as pyrolysis coke but is also often referred to as pyrolysis char. The term “counterflow” (pyrolysis reactor) is to be understood as any kind of pyrolysis reactor where the hot gas is being fed in the bottom of the pyrolysis reactor to drive the pyrolysis process and the resulting gas is drawn from the top of the pyrolysis reactor, while the feedstock is fed at the top of the pyrolysis reactor so that the closer the feedstock moves to the bottom of the pyrolysis reactor the more processed it is. I.e. fuel and gas moves in opposite directions—hence “counterflow” which is also often referred to as “updraft”, “upward draft”, “counter-current” and other. However, in some embodiments a “fixed bed counterflow pyrolysis reactor” can also be arranged tilted or even substantially horizontal, where the feedstock is transported in one direction—e.g. by means of a conveyor or an auger—and hot gas is guided through the feedstock in the opposite direction to pyrolyzer the feedstock as it travels towards the hot gas inlet. I.e. although such a bed of feedstock is constantly moving it is still a fixed bed pyrolysis reactor in that the feedstock is not fluidized during the pyrolysis process. The term “fixed bed” is a known pyrolysis principle in which the feedstock is pyrolyzed by hot gas oozing up through a “solid” pile of feedstock—as opposed to in a fluidized bed reactor where the hot gas is flowing so fast that the feedstock becomes airborne during the pyrolysis process. However, it should be noticed that while the term “fixed bed” excludes pyrolyzing airborne feedstock, the term does also cover embodiments where the fixed bed of feedstock relatively slowly travels downwards as the bottom part of the feedstock pile is turned to coke or char by the pyrolysis process and is removed as it is formed. This “moving bed” design is a specie of the generic term “fixed bed”.
In an aspect, the pyrolysis system further comprises a deoxygenation unit and wherein the deoxygenation unit is arranged to deoxygenate the pyrolysis gas before it enters the first condensing unit.
It is advantageous to deoxygenate the pyrolysis gas before it enters the condensing units in that this will increase the quality of the gas and thereby the gas yield and at least to some degree also increase the quality of the condensed substances depending on the condensation process.
In this context the term “Deoxygenation” refers to a chemical reaction involving the removal of oxygen atoms from a molecule. I.e. the term refers to the removal of molecular oxygen (O2) from the pyrolysis gases and solvents. Deoxygenation can e.g. take place by adding oxygen in some form to pyrolysis gas in a partial oxidation process which will end up deoxygenating the gas, by means of a catalytic process, by means of an oxygen membrane or other.
In an aspect, the deoxygenation unit comprises a partial oxidation unit.
Deoxygenating the pyrolysis gas by means of partial oxidation is advantageous in that the partial oxidation process is a relatively simple and inexpensive way of increasing the quality of the gases and solvents produced in the pyrolysis reactor.
It should be noted that the term “partial oxidation” in this context means that some oxygen is added to the pyrolysis gas but not enough to fully combust the pyrolysis gas completely. I.e. an embodiment enough oxygen is added to combust e.g. 35% of the pyrolysis gas.
In an aspect, the pyrolysis system further comprises an aerosol removal unit arranged to remove aerosol from pyrolysis gas leaving the first condensing unit.
Gas leaving the first condensing unit will typically contain a relatively high amount of oil in aerosol form and if this is not removed before the second condensing unit, the risk of the aerosols settling during the condensing process in the second condensing unit is increased. To ensure that more oil is removed from the gas before the water is separated from the gas in the second condensing unit it is therefore advantageous to arrange an aerosol removal unit between the first and the second condensing unit to remove aerosol from pyrolysis gas leaving the first condensing unit.
In this context the term “aerosol” means a suspension of fine solid particles or liquid droplets in the pyrolysis gas. The liquid or solid particles have diameters typically less than 1 μm. I.e., aerosols are micron and submicron liquid droplets of organic compounds that either have too high a boiling point to evaporate in the pyrolyze reactor or have condensed from vapor after leaving the reactor because the gas stream has cooled. Aerosols tend to consist of carbohydrates, highly substituted phenolic compounds, lignin oligomers etc.
Thus, an “aerosol removal unit” is any type of aerosol remover capable of removing such very fine droplets or particles from the gas flow, such as any kind of electrostatic precipitator, impactors, horizontal elutriators, pore membrane filters and other.
In an aspect, the pyrolysis system further comprises an aerosol removal unit arranged to remove aerosol from pyrolysis gas leaving the second condensing unit.
Aerosols in the pyrolysis gas can settle on pipe wall, in tanks or elsewhere and are in general unwanted in relation to optimal operation of the pyrolysis system and subsequent utilization of the pyrolysis gas. Thus, it is advantageous to arrange an aerosol removal unit at least after the second condensing unit.
In an aspect, the first condensing unit is arranged to cool the pyrolysis gas to a first temperature being above the dew point of water and wherein the second condensing unit is arranged to cool the pyrolysis gas to a second temperature being below the dew point of water.
By arranging the the first condensing unit to cool the pyrolysis gas to a first temperature above the dew point of water it is ensured that water is not condensed in the first condensing unit to produce a valuable first pyrolysis liquid. However, to increase the usability and purity of the pyrolysis gas, also the water has to be removed from the produced pyrolysis gas and it is therefore advantageous to arrange the second condensing unit to cool the pyrolysis gas to a second temperature below the dew point of water.
The dew point of water is in context the temperature to which the gas must be cooled to become saturated with steam. When cooled further, the steam will condense to form liquid water (dew). When the gas containing steam cools to the dew point of water through contact with a surface that is colder than the gas, water will condense on the surface. The dew point of water is also related to the concentration of steam present in the pyrolysis gas. A higher dew point means there is relatively more steam in the pyrolysis gas.
It should be noted that the actual dew point of water obviously is also dependent on the system pressure—i.e. if the pyrolysis system is arranged to operate at around atmospheric pressure, the dew point of water will be at one level and if the pyrolysis system is arranged to operate at a pressure higher than atmospheric pressure, the dew point of water will be at another level. However, the skilled person will know the actual dew point of water at given pressures.
In an aspect, the first condensing unit is arranged to cool the pyrolysis gas to between 50° C. and 200° C., preferably between 65° C. and 160° C. and most preferred between 80° C. and 140° C.
If the first condensing unit is arranged to cool the pyrolysis gas too much the risk of water condensing in the first condensing step—and the thereby not isolate a valuable first pyrolysis liquid—is increased. However, if the first condensing unit is arranged to cool the pyrolysis gas too little the risk of valuable first pyrolysis liquids not being condensed is increased. Thus, the present temperature ranges for the first condensing unit are advantageous in relation to condensing valuable first pyrolysis liquids substantially without condensing water.
In an aspect, the second condensing unit is arranged to cool the pyrolysis gas to between −10° C. and 45° C., preferably between 0° C. and 40° C. and most preferred between 10° C. and 30° C.
If the second condensing unit is arranged to cool the pyrolysis gas too much the process takes too long and requires too much energy. However, if the second condensing unit is arranged to cool the pyrolysis gas too little the risk of water not condensing is increased. Thus, the present temperature ranges for the second condensing unit presents an advantageous relationship between cost and efficiency.
In an aspect, the heating means is arranged to increase the temperature of the pyrolysis gas to between 200° C. and 1,200° C., preferably between 400° C. and 1,000° C. and most preferred between 450° C. and 700° C. before it re-enters the pyrolysis reactor.
If the pyrolysis gas is too cold when it reenters the pyrolysis reactor the pyrolysis process will run slow and inefficient. However, if the pyrolysis gas is too hot when it reenters the pyrolysis reactor, the pyrolysis reactor may be damaged. Thus, the present temperature ranges present an advantageous relationship between efficiency and equipment safety.
In an aspect, the pyrolysis system further comprises flow generating means arranged to drive the portion of the pyrolysis gas through the heating means and further into the pyrolysis reactor and wherein the pyrolysis system also comprises control means arranged to control the flow generating means so that the volume flow rate of the pyrolysis gas is controlled in dependency of input from a temperature measuring device arranged to measure the temperature of the pyrolysis gas at the upper part of the pyrolysis reactor.
Controlling the volume flow rate of the reentered pyrolysis gas in dependency of the temperature of the pyrolysis gas at the upper part of the pyrolysis reactor is advantageous in that this present a simple and efficient way of ensuring more uniform pyrolysis gas and of ensuring that the temperature of the pyrolysis gas leaving the pyrolysis reactor is at a desirable low level to ensure efficient condensation in the subsequent condensation processes.
It should be noted that the term “flow generating means” in this context should be understood as any type of flow generator capable of driving at least a portion of the pyrolysis gas through the heating means—e.g. any kind of fan, pump, flow driver or other.
It should also be noted that the term “heating means” in this context should be understood as any type of heater capable of increasing the temperature of the pyrolysis gas, such as any kind of combustion heater, heat exchanger, electrical heater or other.
Further, it should be noted that the term “control means” in this context should be understood as any type of controller capable of controlling operations of the pyrolysis system, such as any kind of computer, programmable logic controller (PLC), logical circuit or other.
In an aspect, the pyrolysis gas outlet is connected to filtering means arranged to separate particles from pyrolysis gas flowing out through the pyrolysis gas outlet.
It is advantageous to filter the pyrolysis gas in that the risk of unwanted particle build-up in the system is hereby reduced.
In this context, the term “filtering means” is to be understood as any kind of filter suitable for separating particles from the pyrolysis gas leaving the pyrolysis reactor—i.e. any kind of cyclone, sieve, strainer or another device for cleaning the pyrolysis gas flow.
In an aspect, between 1% and 95%, preferably between 5% and 70% and most preferred between 10% and 50%—such as between 20% to 30%—of the pyrolysis gas produced by the feedstock in the pyrolysis reactor is circulated back into the pyrolysis reactor to form a flow of pyrolysis gas up through the feedstock.
If too much or too little of the pyrolysis gas is circulated back into the pyrolysis reactor, the pyrolysis reactor will run more inefficiently. Thus, the present amount ranges will ensure higher efficiency.
The invention also provides for a method for producing purified pyrolysis gas and pyrolysis liquids, the method comprising the steps of:
Forming the pyrolysis gas in a fixed bed counterflow pyrolysis reactor and subsequently condensing pyrolysis liquids in at least two stages at different temperatures is advantageous in that the fixed bed counterflow pyrolysis ensures a relative low temperature of the pyrolysis gas ensuring that the risk of settling of unwanted substances in the system before and in the condensers is reduced and it ensures that the pyrolysis liquids can be condensed at a better quality. Thus, ensuring both better pyrolysis liquids and more pure pyrolysis gas. And by using produced pyrolysis gas to drive the pyrolysis process in the pyrolysis reactor a more simple and efficient process is achieved.
It should be noticed that the above listing of method step is not limited to a specific order. It should particularly be noted that the drawing, heating and reentering a portion of the pyrolysis gas can be done at different stages of the process—i.e. both before and after the condensation process.
In an aspect, the pyrolysis gas is deoxygenated before it enters the first condensing unit.
It is advantageous to deoxygenate the pyrolysis gas before it enters the condensing units in that this will increase the quality of the gas and thereby the gas yield and at least to some degree also increase the quality of the condensed substances depending on the condensation process.
In an aspect, the pyrolysis gas is deoxygenated through partial oxidation.
Partial oxidation is an inexpensive and reliable way of deoxygenating the pyrolysis gas.
In an aspect, aerosol is removed from the pyrolysis gas leaving the first condensing unit before it enters the second condensing unit.
Gas leaving the first condensing unit will typically contain a relatively high amount of oil in aerosol form and if this is not removed before the second condensing unit, the risk of the aerosols settling during the condensing process in the second condensing unit is increased. To ensure that more oil is removed from the gas before the water is separated from the gas in the second condensing unit it is therefore advantageous to arrange an aerosol removal unit between the first and the second condensing unit to remove aerosol from pyrolysis gas leaving the first condensing unit.
In an aspect, aerosol is removed from the pyrolysis gas leaving the second condensing unit.
Aerosol may settle in the system and thereby decrease the systems efficiency or even clog the system. Thus, it is advantageous to remove any aerosol from the pyrolysis gas after it leaves the second condensing unit.
In an aspect, the pyrolysis gas is cooled in the first condensing unit to a first temperature being above the dew point of water.
Cooling the pyrolysis gas to a first temperature above the dew point of water in a first step is advantageous in that valuable pyrolysis gas fluids hereby can be condensed and isolated—i.e., the valuable pyrolysis gas fluids can be produced substantially free of any condensed water.
In an aspect, the pyrolysis gas is cooled in the second condensing unit to a second temperature being below the dew point of water.
To produce valuable pyrolysis gas it is important that also the steam produced in the pyrolysis reactor is condensed and it is therefore advantageous pyrolysis gas is cooled to a second temperature being below the dew point of water in a second condensing step.
In an aspect, the pyrolysis gas is cooled in the first condensing unit to between 50° C. and 200° C., preferably between 65° C. and 160° C. and most preferred between 80° C. and 140° C.
If the pyrolysis gas is cooled too much in the first condensing step the risk of water condensing in the first condensing step—and the thereby not isolate a valuable first pyrolysis liquid—is increased. However, if the pyrolysis gas is cooled too little in the first condensing step, the risk of valuable first pyrolysis liquids not being condensed is increased. Thus, the present temperature ranges for the first condensing step are advantageous in relation to condensing valuable first pyrolysis liquids substantially without condensing water.
In an aspect, the pyrolysis gas is cooled in the second condensing unit to between−10° C. and 45° C., preferably between 0° C. and 40° C. and most preferred between 10° C. and 30° C.
If the pyrolysis gas is cooled too much in the second condensing step the process takes too long and requires too much energy. However, if the pyrolysis gas is cooled too little the risk of water not condensing is increased. Thus, the present temperature ranges for the second condensing step presents an advantageous relationship between cost and efficiency.
In an aspect, the temperature of the pyrolysis gas is increase by the heating means to between 200° C. and 1,200° C., preferably between 400° C. and 1,000° C. and most preferred between 450° C. and 700° C. before it re-enters the pyrolysis reactor.
If the pyrolysis gas is too cold when it re-enters the pyrolysis reactor the pyrolysis process will run slow and inefficient. However, if the pyrolysis gas is too hot when it re-enters the pyrolysis reactor, the pyrolysis reactor may be damaged. Thus, the present temperature ranges present an advantageous relationship between efficiency and equipment safety.
In an aspect, the volume flow rate of the heated pyrolysis gas being guided back into the pyrolysis reactor through the pyrolysis gas inlet is controlled in dependency of the temperature of the pyrolysis gas at the upper part of the pyrolysis reactor.
Controlling the amount of heated pyrolysis gas entering the pyrolysis reactor on the basis of the temperature of the pyrolysis gas at the upper part of the pyrolysis reactor— and thereby the temperature of the pyrolysis gas exciting the pyrolysis reactor—is advantageous for at least two reasons. This will ensure that a constant exit temperature of the pyrolysis gas from the pyrolysis reactor can be maintained which will improve the yield of the subsequent condensing steps and simplify the control of the condensing steps. Furthermore, controlling the amount of heated pyrolysis gas entering the pyrolysis reactor on the basis of the temperature of the pyrolysis gas at the upper part of the pyrolysis reactor is advantageous in that this will ensure a constant and efficient pyrolysis process in the pyrolysis reactor no matter how much and which type and quality of feedstock is fed into the pyrolysis reactor.
In an aspect, particles are separated from pyrolysis gas flowing out through the pyrolysis gas outlet by means of filtering means.
To increase the purity of the subsequently condensed fluids and the produced pyrolysis gas it is advantageous to remove any particles—such as ash—before the pyrolysis gas produced in the pyrolysis reactor enters the condensing steps.
In an aspect, between 1% and 95%, preferably between 5% and 70% and most preferred between 10% and 50%—such as between 20% to 30%—of the pyrolysis gas produced by the feedstock in the pyrolysis reactor is circulated back into the pyrolysis reactor to form a flow of pyrolysis gas up through the feedstock.
If too much or too little of the pyrolysis gas is circulated back into the pyrolysis reactor, the pyrolysis reactor will run more inefficiently. Thus, the present amount ranges will ensure higher efficiency.
The invention further provides for use of a pyrolysis system according to any of the previously discussed pyrolysis systems for pyrolyzing biomass.
Pyrolyzing and/or gasification of biomass is problematic in relation to tar content in the resulting gas and it is therefore particularly advantageous to use the present invention in relation to pyrolyzing and/or gasification of biomass.
It should be emphasised that the term “biomass” in this context should be understood as any kind of plant or animal material suitable for energy conversion in a fixed bed counterflow pyrolysis reactor of a pyrolysis system according to the present invention. Thus, the term covers any kind of chipped, pelletized or whole wood, nutshell, pip, peat, grain or other biomass materials that will not cake when being fed down into the reactor and thereby allowing the hot pyrolysis gas to flow substantially evenly and well distributed up through the biomass in the reactor.
The invention will be described in the following with reference to the figures in which
In this embodiment feedstock 19 is guided into the pyrolysis reactor 2 through a feedstock inlet 11 at an upper part 8 of the pyrolysis reactor 2.
It should be noticed that any reference to orientation throughout this document—such as upper, lower, up, down etc.—relates to the orientation of the system 1 during normal use under normal circumstances. I.e., the term “upper part 8 of the pyrolysis reactor 2” refers to the top part of the pyrolysis reactor 2—such as the upper 30%, the upper 20% or the upper 10% of the total vertical extend of the pyrolysis reactor 2 and the term “lower part 10 of the pyrolysis reactor 2” refers to the bottom part of the pyrolysis reactor 2—such as the bottom 30%, the bottom 20% or the bottom 10% of the total vertical extend of the pyrolysis reactor 2.
In this embodiment, the feedstock 19 is wood chips but in another embodiment the feedstock 19 could be nut shells, corn cops, fruit pips or stones, grains, pelletized straw material or any other type of biomass or it could surplus material from biochemical production or food production, treaded or torn waste material or any other form of organic material, plastic material or fossil fuel that can be used for energy conversion in a pyrolysis system 1.
At the top 8 of the pyrolysis reactor 2 the operation temperature will typically be around 150-250° C. but as the feedstock 19 moves downwards inside the pyrolysis reactor 2 the temperature rises to 500° C. or more at the bottom 6 of the pyrolysis reactor 2. At the lower part 10 of the pyrolysis reactor 2 the feedstock 19 is transformed into pyrolyzed char (also called coke) and it will fall through a grate device 22 on which the feedstock 19 rests in the pyrolysis reactor 2 and continue out of the pyrolysis reactor 2 through the char outlet 12. In this embodiment the grate device 22 is formed by a number of transversal profiles that can be moved to incite the char to fall through at a slow pace to avoid un-pyrolyzed feedstock to fall through. However, in another embodiment the grate device 22 could also or instead comprise one or more passive grates and/or it could also or instead comprise other forms of moving grate elements.
Although the feedstock 19 is moving slowly downwards as it is being pyrolyzed in the reactor 1 this reactor 2 still falls under the term “a fixed bed counterflow pyrolysis reactor” 2 in that a fixed bed of feedstock 19 is continuously maintained in the reactor 2—i.e., the feedstock 19 is not fluidized or in other ways airborne while being pyrolyzed. This type of reactor 2 is also sometimes referred to as a moving bed reactor 2 which is a species of the generic term “fixed bed pyrolysis reactor”.
In this embodiment the char outlet 12 comprises a sluice device 23 arranged to allow the generated char to move downwards and out of the reactor 2, while at the same time ensuring that gas does not escape. In this embodiment the sluice device 23 is a gas lock but in another embodiment the sluice device 23 could also or instead comprise a register, a gate, a lock or other.
In the pyrolysis reactor 2 the produced pyrolysis gas will travel upwards through and in direct contact with the feedstock 19 and leave the pyrolysis reactor 2 through the pyrolysis gas outlet 7. From there most of the pyrolysis gas continues into the condensation stages while a portion of the pyrolysis gas drawn into a return conduit 5 by means of flow generating means 16 and further through heating means 6 in which the gas is heated to a temperature of 500-600 degrees Celsius before reentering the pyrolysis reactor 2 at the lower part 10 of the reactor 2. In this embodiment the flow generating means 16 comprises a fan but in another embodiment the flow generating means 16 could comprise a pump or another type of flow generator. Or, in another embodiment the flow of pyrolysis gas through the pyrolysis system 1 could also or instead be driven by the pressure generated by the pyrolysis process in the pyrolysis reactor 2.
In this embodiment, the heated pyrolysis gas reenters the pyrolysis reactor 2 through a pyrolysis gas inlet 9 arranged at the lower part 10 of the reactor 2 just below the grate device 22 but in another embodiment the pyrolysis gas inlet 9 could be arranged just above the grate device 22 or several pyrolysis gas inlets 9 could be arranged below and/or just above the grate device 22 e.g. to distribute the heated pyrolysis gas more evenly in the feedstock 19.
In this embodiment of the invention the pyrolysis system 1 further comprises filtering means 20 arranged immediately after the pyrolysis gas outlet 7 in which dust and minor particles are removed from the gas. In this embodiment the filtering means 24 are arranged immediately after the pyrolysis gas outlet 7 but in another embodiment it could also or instead be arranged after the condensation stages, between the stages or elsewhere in the system 1.
In this embodiment, the recycled pyrolysis gas is heated by means of heating means 6 in the form of a heat exchanger 6 enabling that the pyrolysis gas is being heated by exchanging heat with an external hot fluid but in another embodiment the heating means 6 could heat the recycled pyrolysis gas by partial oxidation or by means of another internal heat source—such as combustion of the finished gas product—or by means of another external heat source.
In this embodiment the part of the pyrolysis gas that is not recycled will continue into a first condensing unit 3 in which the pyrolysis gas is cooled to a first temperature to condense a first pyrolysis liquid 20. From there the pyrolysis gas continues into a second condensing unit 4 in which the pyrolysis gas is cooled to a second temperature to condense a second pyrolysis liquid 21 and from there the pyrolysis gas continues into a third condensing unit 25 in which the pyrolysis gas is cooled to a third temperature to condense a third pyrolysis liquid 26. Different substances in the pyrolysis gas will condense at different temperatures and the more condensation stages operating at different gradually decreasing temperatures the purer pyrolysis liquids can be produced in the condensation process. Most of the substances in the pyrolysis gas will have a condensation temperature above the dew point of water and it is therefore advantageous that at least the first condensing unit 3 will cool the pyrolysis gas to a first temperature above the dew point of water to produce a first pyrolysis liquid 20 being free of water. In this embodiment the first condensing unit 3 will cool the pyrolysis gas to 105° C. but in another embodiment the first condensing unit 3 could cool the pyrolysis gas to 100° C., 95° C., 85° C. or even lower or to 120° C., 160° C., 180° C. or even higher depending on the specific feedstock 19, the pressure inside the condensing unit 3, the amount of steam in the produced pyrolysis gas or other.
The pyrolysis of the feedstock 19 will produce a large amount of steam which has to be removed from the pyrolysis gas before the gas can be used for heating, as a liquid fuel or other and it is therefore advantageous that the condensation process comprises a second condensing unit 4 in which the pyrolysis gas is cooled to a second temperature below the dew point of water to condense a second pyrolysis liquid 21 which will contain a lot of water. In this embodiment the second condensing unit 4 will cool the pyrolysis gas to 20° C. but in another embodiment the second condensing unit 4 could cool the pyrolysis gas to 15° C., 10° C., 5° C. or even lower or to 30° C., 60° C., 80° C. or even higher depending on the specific feedstock 19, the pressure inside the condensing unit 3, the amount of steam in the produced pyrolysis gas or other.
In this embodiment the gas will further pass through a third condensing unit 25 in which the pyrolysis gas is cooled to a third temperature further below the dew point of water to condense a third pyrolysis liquid 26 consisting of substances having a dew point further below the dew point of water. In this embodiment the third condensing unit 25 will cool the pyrolysis gas to 0° C. but in another embodiment the third condensing unit 25 could cool the pyrolysis gas to −10° C., −20° C., −30° C. or even lower or to 5° C., 10° C., 15° C. or even higher depending on the specific feedstock 19, the pressure inside the condensing unit 3, the amount of steam in the produced pyrolysis gas or other. Thus, in this embodiment the pyrolysis system 1 comprises three independent condensation stages 3, 4, 25 but in another embodiment the pyrolysis system 1 would only comprise the first condensing unit 3 and the second condensing unit 4 or the pyrolysis system 1 would comprise more than three condensation stages such as four, five, six or even more.
In this embodiment the first condensing unit 3, the second condensing unit 4 and the third condensing unit 25 comprises cooling means 29 or a cooler 29 in the form of surrounding outer shells 30 through which a cooling fluid may flow to exchange heat with the passing pyrolysis gas and thereby cool the pyrolysis gas to the desired temperature level in each condensing unit 3, 4, 25. However, in another embodiment the cooling means could also or instead comprise passive heat exchanging means such as heat sinks, active closed cooling circuits comprising compressor etc. and/or the pyrolysis gas could be cooled in one or more of the condensing units 3, 4, 25 to the desired temperature level in any other way known to the skilled person.
In this embodiment the pyrolysis gas leaving the last condensation stage 25 will continue into an aerosol removal unit 15 arranged to remove aerosol from the pyrolysis gas. In this embodiment the aerosol removal unit 15 comprises a wet electrostatic precipitator but in another embodiment the aerosol removal unit 15 could also or instead comprise multiple vortex chambers, a dry electrostatic precipitator or other.
In this embodiment the aerosol removal unit 15 is only arranged after the last condensation stage 25 but in another embodiment the pyrolysis system 1 could also or instead comprise an aerosol removal unit 15 before the first condensation stage 3 or after each condensation stage 3, 4, 25. In fact it is particularly advantageous to also or instead to arrange an aerosol removal unit 15 after the first condensation stage 3 so that it may remove valuable first pyrolysis liquid—i.e., typically oil—from the gas before it enters the second condensing unit 4 to ensure that the oil aerosols do not settle or condense in the subsequent condensing steps.
In this embodiment the pyrolysis gas leaving the pyrolysis reactor 2 is guided through the condensation stages 3, 4, 25 and the aerosol removal unit 15. From the aerosol removal unit 15 the now purified gas enters the return conduit 5 where a portion of the purified gas is heated before it reenters the pyrolysis reactor 2.
In the embodiment disclosed in
In this embodiment the pyrolysis gas is first lead through a deoxygenation unit 13 before it enters the condensation stages 3, 4, 25. In this embodiment the deoxygenation unit 13 is a partial oxidation unit 14 but in another embodiment the deoxygenation could also or instead take place through a catalytic process.
In the partial oxidation unit 14 the pyrolysis gas is partially oxidized in that air, oxygen enriched air, a mixture of oxygen and CO2 or other or pure oxygen is added to the pyrolysis gas through the oxidation inlet 28 so that a part of the pyrolysis gas is combusted, which in turn will raise the temperature of the gas. This temperature elevation and the partial combustion process will among other ensure an advantageous tar decomposition.
In this embodiment enough oxygen is added to combust approximately 35% of the pyrolysis gas. However, in another embodiment the partial oxidation involves adding enough oxygen to combust all the pyrolysis gas between 10% and 60%, preferably between 25% and 50%. The present amount ranges are advantageous in relation to tar decomposition.
In this embodiment the pyrolysis system 1 comprises control means 17 arranged to control the flow generating means 16 so that the volume flow rate of the pyrolysis gas is controlled in dependency of input from a temperature measuring device 18 arranged in the upper part 8 of the pyrolysis reactor 2 to measure the temperature of the pyrolysis gas at the upper part 8 of the pyrolysis reactor 2. Thus, if the temperature of the pyrolysis gas in the upper part 8 of the pyrolysis reactor 2 becomes too low the control means 17 will increase the volume flow rate of the hot reentered pyrolysis gas and if the temperature of the pyrolysis gas in the upper part 8 of the pyrolysis reactor 2 becomes too high the control means 17 will decrease the volume flow rate of the hot reentered pyrolysis gas. However, in another embodiment the control means 17 could also or instead be arranged to control the temperature of the pyrolysis gas at the upper part 8 of the pyrolysis reactor 2 by controlling the feedstock level in the pyrolysis reactor 2, by controlling to which temperature the recycled pyrolysis gas is heated by the heating means, by controlling the pressure in the pyrolysis system by means of a reduction valve (not shown) or other.
The invention has been exemplified above with reference to specific examples of pyrolysis reactors 2, condensing units 3, 4, 25, aerosol removal units 15 and other. However, it should be understood that the invention is not limited to the particular examples described above but may be designed and altered in a multitude of varieties within the scope of the invention as specified in the claims.
| Number | Date | Country | Kind |
|---|---|---|---|
| 20154881.5 | Jan 2020 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/DK2021/050028 | 1/28/2021 | WO |
