Patent Application
20230220432
The present disclosure generally relates to a method for preparing an SO2 based liquid derivable from an acidified lignocellulosic biomass, to a method for preparing an SO2 gas stream derivable from an acidified lignocellulosic biomass, and to a system for treatment of lignocellulosic biomass.
Lignocellulosic residues from forestry are attractive as feedstocks for the production of green chemicals and fuels, since they are abundant, relatively inexpensive, and not used for food. Lignocellulose consists mainly of lignin and two classes of polysaccharides, cellulose and hemicellulose. The polysaccharides can be hydrolyzed to sugars and converted to various fermentation products, e.g. bioalcohols, by means of fermenting microorganisms, such as Saccharomyces cerevisiae.
The hydrolysis of cellulose is typically preceded by a pretreatment process, in which the hemicellulose is degraded, and the cellulose is made more accessible to cellulolytic enzymes. During hydrolysis, the cellulose present is partly converted into reducing sugars.
The pretreatment process is typically carried out in a pretreatment arrangement, comprising an impregnation vessel and a reactor vessel. In the impregnation vessel, the biomass is impregnated with an additive facilitating degradation of the biomass, and in the reactor vessel the degradation is improved by exposing the biomass to an elevated temperature and pressure. The pretreatment arrangement also generally comprises an inlet for receiving the biomass to be pretreated and an outlet for discharging the pretreated biomass, typically as a biomass slurry. The overall aim of the pretreatment is to disrupt the crystalline cellulose structure and to remove or partially remove lignin from the lignocellulosic biomass. The pretreatment process is complex and involves many reactions and side-reactions. Such reactions may result in the formation of various by-products, which may be inhibitory to downstream processes. Furthermore, volatile compounds and gases contained in the lignocellulose biomass are set free when the material is degraded or partially degraded. Correspondingly, the hydrolysis is typically carried out in a hydrolysing unit and the fermentation in a fermentation unit or fermentation vessel.
The overall process, from the pre-treatment to the fermentation, is relatively complex and may comprise the addition of additives and various process streams such as water and steam. Moreover, the preferred conditions for optimizing the degradation of the biomass varies along the process. For example, in some process steps, a high amount of liquid is preferred for optimal treatment of the biomass material, while in other process steps, superfluous liquid results in unnecessary costs. Moreover, for environmental reasons, cleaning and/or removal of certain substances used, or produced, in the process are often needed. All of the above results in additional costs, and adds complexity to the process.
There is thus a need for improvements with respect to the process which allows for a more cost efficient and/or in at least some aspects less complicated system.
In view of the above, it is an object of the present invention to provide improvements with respect to methods and arrangements for the treatment of lignocellulosic biomass, particularly to achieve a less costly process, and/or in at least some aspects, a less complicated system.
According to a first aspect of the present invention, a method for preparing an SO2 based liquid derivable from an acidified lignocellulosic biomass is provided. The method comprising the steps of:
pretreating a lignocellulosic biomass material in a pretreatment arrangement, the pretreating including treating the lignocellulosic biomass material with SO2 and subjecting SO2 impregnated biomass to an elevated temperature and pressure in a reactor vessel of the pretreatment arrangement to provide a pretreated biomass slurry;
optionally hydrolyzing the pretreated biomass slurry in a hydrolysis unit with at least one aqueous hydrolyzing liquid, comprising saccharification enzymes, under conditions in which at least a part of the pretreated biomass slurry is hydrolyzed to a hydrolysate, said hydrolysate comprising fermentable sugars and inhibitory substances;
retrieving gaseous SO2 from the pretreatment arrangement to provide an SO2 gas stream;
treating the SO2 gas stream with an alkaline solution to provide a sulfite/bisulfite solution;
supplying at least a part of the sulfite/bisulfite solution to at least one of:
Hereby, an efficient yet simple way of re-using at least some substances from the process are provided. Besides the advantageous effects presented below for each one of the options a)-d), by re-using at least some substances a cost-effective process is provided. Moreover, by re-using at least some substances from the process, required cleaning and removal of substances e.g. due to emission restrictions, can be reduced or even omitted. In particular, the invention provides in addition to the process advantages also an efficient way of reducing SO2 (sulfur dioxide) related emissions.
The sulfite/bisulfite solution may thus be used in the process according to any one of (e.g. according to several of) options a)-d). Stated differently, the method comprises the step of supplying at least a part of the sulfite/bisulfite solution to the process upstream of, to, and/or downstream of the pretreatment of the lignocellulosic biomass material. At least a part of the sulfite/bisulfite solution may e.g. be at least 50%, or at least 75%, such as e.g. approximately 100% or 100% of the sulfite/bisulfite solution. According to at least one example embodiment, at least a part of the sulfite/bisulfite solution is less than 50%, or less than 25%, such as e.g. approximately 10% of the sulfite/bisulfite solution.
By providing a sulfite/bisulfite solution which is supplied to any one of, or several of, options a)-d), a flexible and versatile way of re-using at least some substance from the process are provided. That is, by providing a sulfite/bisulfite solution which may be used for different purposes in the process depending on the point of application, and supplying the sulfite/bisulfite solution to one of, or several of, options a)-d), a flexible and versatile way of re-using at least some substance from the process are provided. Thus, the sulfite/bisulfite, and the supply thereof to any one of, or several of, options a)-d) may be adapted based on the need of the process.
According to at least one example embodiment, the method comprises in a first time period, supplying the sulfite/bisulfite solution by means of one of, or several of, options a)-d), and in a second time period, supplying the sulfite/bisulfite solution by means of one of, or several of, options a)-d) at least partly different to the supply of the sulfite/bisulfite solution in the first time period. Thus, the supply of the sulfite/bisulfite solution by means of one of, or several of, options a)-d) may vary over time. For example, in the first time period, the sulfite/bisulfite is supplied by means of only one of the options a)-d) as this is where the re-use of the substance from the process is deemed to be most efficient for the particular first time period. Subsequently, in the second time period, supply of the sulfite/bisulfite by means of another, or an additional, option a)-d), is achieved, or alternatively at least two other options of a)-d) are achieved, as this is where the re-use of the substance from the process is deemed to be most efficient for the particular second time period.
According to at least one example embodiment, the method comprises varying the supply of the sulfite/bisulfite solution between one or more of the options a)-d) over time. Thus, the method may be adapted based on the needs of the process over time.
According to at least one example embodiment, the method comprises supplying at least a part of the sulfite/bisulfite solution to at least two of the options a)-d). Hereby, the sulfite/bisulfite solution can be distributed to the at least two options a)-d) depending on the need of the process. In other words, by providing a sulfite/bisulfite solution, re-use of at least some substance from the process may be distributed and divided in an easy manner between one or more of the different options of a)-d).
By providing a sulfite/bisulfite solution for re-using at least some substances from the process, not only sulphur but additional alkali substances from the treatment of the SO2 gas stream with an alkaline solution, may be re-used in the process. Moreover, a sulfite/bisulfite solution is in at least some aspects easier to handle compared to a gaseous SO2 stream, as the latter is e.g. hazardous and corrosive. Moreover, by providing the substances to be re-used in the process as a sulfite/bisulfite solution instead of e.g. a gas stream, relative straightforward process equipment can be used, as e.g. transportation pipelines, pumps and valves configured to handle liquids. Thus, according to at least one example embodiment, the method comprises supplying at least a part of the sulfite/bisulfite solution to at least one of options a)-d) by means of a transportation pipe and a pump configured to move a liquid, such as the sulfite/bisulfite solution, in the transportation line. The transportation line is typically arranged between the process equipment treating the SO2 gas stream with an alkaline solution to provide the sulfite/bisulfite solution (e.g. a scrubber as described more in detail later) and at least on point in the process corresponding to at least one of options a)-d). Additionally, one or more valves for handling liquids, such as the sulfite/bisulfite solutions, is arranged along the transportation line.
According to at least one example embodiment, the steps of: retrieving gaseous SO2 from the pretreatment arrangement to provide an SO2 gas stream; treating the SO2 gas stream with an alkaline solution to provide a sulfite/bisulfite solution; and supplying at least a part of the sulfite/bisulfite solution to at least one of options a)-d) are performed subsequently in the order as presented.
According to at least one example embodiment, the step of pretreating the lignocellulosic biomass material in a pretreatment arrangement comprises treating the lignocellulosic biomass material with SO2 in an impregnation vessel of the pretreatment arrangement, and subjecting SO2 impregnated biomass from the impregnating step to the elevated temperature and pressure in the reactor vessel. According to at least one example embodiment, the step of pretreating the lignocellulosic biomass material in a pretreatment arrangement comprises providing SO2 pre-impregnated lignocellulosic biomass and subjecting the SO2 pre-impregnated lignocellulosic biomass to the elevated temperature and pressure in the reactor vessel.
In accordance with option a) the sulfite/bisulfite solution is used at least to impregnate the lignocellulosic biomass material in order to facilitate the mechanism in which the hemicellulose is degraded, and the cellulose is made more accessible to cellulolytic enzymes. Moreover, by impregnating the lignocellulosic biomass prior to the pretreatment arrangement, less SO2 may be needed in the impregnation step in the pretreatment, or the impregnation step in the pretreatment may be omitted. Thus, according to at least one example embodiment, the impregnation step using SO2 in the pretreatment arrangement may be omitted, and the sulfite/bisulfite treated lignocellulosic biomass material may be supplied directly to the reactor vessel of the pretreatment arrangement.
In accordance with option b) the sulfite/bisulfite solution may be used to impregnate the lignocellulosic biomass material for the same reasons mentioned in option a), but by supplying the sulfite/bisulfite solution to the lignocellulosic biomass material in the pretreatment arrangement, e.g. into the impregnation vessel. Here, the sulfite/bisulfite solution may be used as a complement to the SO2 supplied to the impregnation vessel. Additionally or alternatively, the sulfite/bisulfite solution can be supplied to the reactor vessel as makeup liquid (for dilution). Hereby, SO2 can be re-used in the process, as well as reducing the need of other makeup liquids (as e.g. makeup water). Moreover, this may lead to a reduced need of handling residue liquids, such as residue water, downstream of the pretreatment arrangement.
In accordance with options a) and/or b), the sulfite/bisulfite solution is typically subject to an environment with a low pH and/or high temperature, either as a direct effect of the point of application/supply (i.e. at a) or b)) or as a separate means arranged prior to the point of application/supply, which results in the formation of SO2 in gaseous form, facilitating impregnation and/or reaction with the lignocellulosic biomass material.
In accordance with option c) the sulfite/bisulfite solution is used at least to modify the characteristics of the pretreated biomass slurry prior to subjecting it to downstream process steps. Such modification is desired as the pretreated biomass slurry typically is not optimized for the downstream process steps, which is further discussed below. The supply of the sulfite/bisulfite solution according to option c) may be performed by supplying the sulfite/bisulfite solution to a process location downstream the reactor vessel, e.g. between the reactor vessel and the hydrolyzing unit.
In accordance with option d) the sulfite/bisulfite solution may be used at least to prevent undesired microbial growth of the fermentable sugars to facilitate storing of the same. For example, the fermentable sugars may initially be brought to a higher concertation than the target concentration, and subsequently be subject to dilution by the sulfite/bisulfite solution to reach the target concentration while additionally providing for the previously mentioned prevention of undesired microbial growth.
According to at least one example embodiment, the method comprises the step of detoxifying the hydrolysate by decreasing the concentration of at least one of the inhibitory substances using the sulfite/bisulfate solution.
Hereby, the resulting hydrolysate is less toxic with regards to yeast and/or other enzymes used in downstream process steps. It should be noted that the inhibitory substances are typically still present in the hydrolysate after the dilution with the sulfite/bisulfite solution, but that the inhibitory substances undergo reactions resulting in less toxic states.
According to at least one example embodiment, the step of detoxifying the hydrolysate is carried out by option c) above. However, it should be noted that any upstream supply of the sulfite/bisulfite solution at least to some extent contributes to the advantageous effects mentioned in relation to any downstream option of supply of the sulfite/bisulfite. For example, even if the sulfite/bisulfite solution is supplied in accordance with option a) or b) the advantageous effects of option c) or the detoxification of the hydrolysate, are still to at least some degree met, as the substances of the sulfite/bisulfite solution are following the flow of biomass further downstream of the point of application.
According to at least one example embodiment, the method comprises the step of increasing the pH of the pretreated biomass slurry to between 4 and 6, using the sulfite/bisulfite solution.
Hereby, a desired pH, e.g. with regards to preferred pH for enzymes, for the downstream process steps is provided. Moreover, the use of another means, such as e.g. an alkaline solution, for increasing the pH can be reduced or even omitted. However, it should be understood that the sulfite/bisulfite solution may be used together with such means (e.g. another alkaline solution) to reach the desired pH. For example, the sulfite/bisulfite solution may have a pH between 4 and 7, such as e.g. between 5 and 6, while the pretreated biomass slurry may have a pH of between 1 and 2, such as e.g. between 1.3 and 1.8. By an appropriate amount of sulfite/bisulfite solution, and possibly another alkaline solution, the target pH may be reached.
According to at least one example embodiment, the method comprises the step of increasing the pH of the pretreated biomass slurry to between 3 and 7, using the sulfite/bisulfite solution.
Hereby, the process can be adapted based on the pH with regards to preferred environment for various enzymes. For example, a relatively high pH may be desired if cellulolytic bacteria or fungi is used in downstream process steps.
It should be noted that SO2 can be retrieved from other process steps besides the pretreatment arrangement, e.g. the hydrolysis step or any fermentation step, or any auxiliary equipment arranged in between, e.g. a flash tank. The SO2 retrieved from the process is typically excess gaseous SO2.
According to at least one example embodiment, retrieving gaseous SO2 from the pretreatment arrangement to provide an SO2 gas stream is at least partly performed by retrieving SO2 gas from the reactor vessel of the pretreatment arrangement. Hereby, excess SO2 can relatively easily be retrieved from the process. For example, the reactor vessel comprises a gas valve, preferably arranged at an upper half of the reactor vessel, typically at the head space of the reactor vessel, the gas valve being configured to discharge SO2 gas from the reactor vessel. The gas valve may be further connected to a gas transportation line configured to transport the SO2 gas to the process equipment treating the SO2 gas stream with an alkaline solution to provide the sulfite/bisulfite solution (e.g. a scrubber as described more in detail later).
According to at least one example embodiment, the step of treating the SO2 gas stream with an alkaline solution is performed in an SO2 scrubber.
Hereby, a well-suited equipment can be used to produce the sulfite/bisulfite solution. An SO2 scrubber is moreover relatively easy to implement in the process as it is adapted for separated streams of SO2 and alkaline solution. Moreover, the resulting sulfite/bisulfite solution is relatively easy withdrawn from the SO2 scrubber and can thus be used in the process accordingly.
According to at least one example embodiment, the method comprises the step of separation of the pretreated biomass slurry to remove a liquid fraction.
For example, the liquid fraction may be removed from the process, and the solid fraction may be used in the downstream process steps. Hereby, the process can be carried out in a more efficient manner. It should be noted that in embodiments with such separation, the supply of the sulfite/bisulfite solution according to option c) may be performed by supplying the sulfite/bisulfite solution to a process location between the reactor vessel and the separation.
According to at least one example embodiment, the method comprises a steam explosion step, preferably arranged downstream of the reactor vessel.
Hereby the biomass material is further disintegrated facilitating the degradation process.
According to at least one example embodiment, the method comprises subjecting the fermentable sugars of the hydrolysate to fermentation in an aqueous liquid utilizing at least one fermenting microorganism under conditions in which at least a part of the fermentable sugars is fermented into a primary target chemical.
Such fermentation may e.g. be carried out in a fermentation unit or fermentation vessel. The primary target chemical may e.g. be ethanol.
According to at least one example embodiment, retrieving gaseous SO2 from the pretreatment arrangement to provide an SO2 gas stream is at least partly performed by retrieving SO2 gas from the steam explosion step. Hereby, excess SO2 can relatively easily be retrieved from the process, as the steam explosion step provides the necessary pressure reduction for SO2 to be released as SO2 gas. According to at least one example embodiment, retrieving gaseous SO2 from the pretreatment arrangement to provide an SO2 gas stream is at least partly performed by retrieving SO2 gas from the reactor vessel and the steam explosion step. Hereby, SO2 gas is retrieved from at least two different positions in the process. The amount of SO2 gas in the SO2 gas stream is e.g. between 1 and 5 wt %, such as e.g. between 3 and 5 wt %.
According to at least one example embodiment, retrieving the gaseous SO2 from the pretreatment arrangement is achieved by retrieving the gaseous SO2 at predetermined process positions. Hereby, the retrieving of the gaseous SO2 can be performed in a controlled and stable manner. The predetermined process positions may e.g. be a process position at which the pH is known, or intentionally adjusted.
According to at least a second aspect of the present invention, a method for preparing a SO2 gas stream derivable from an acidified lignocellulosic biomass is provided. The method comprising the steps of:
pretreating a lignocellulosic biomass material in a pretreatment arrangement the pretreating including treating the lignocellulosic biomass material with SO2 in an impregnation vessel of the pretreatment arrangement, and subjecting SO2 impregnated biomass from the impregnating step to an elevated temperature and pressure in a reactor vessel of the pretreatment arrangement to provide a pretreated biomass slurry;
optionally hydrolyzing the pretreated biomass slurry in a hydrolysis unit with at least one aqueous hydrolyzing liquid, comprising saccharification enzymes, under conditions in which at least a part of the pretreated biomass slurry is hydrolyzed to a hydrolysate, said hydrolysate comprising fermentable sugars and inhibitory substances;
retrieving gaseous SO2 from the pretreatment arrangement to provide an SO2 gas stream;
treating the SO2 gas stream with an alkaline solution to provide a sulfite/bisulfite solution;
treating the sulfite/bisulfite solution to form a separated gas stream;
using the separated gas stream in at least one of the following processes:
Effects and features of the steps of pretreating, optionally hydrolyzing, retrieving gaseous SO2 and treating the SO2 gas stream with an alkaline solution in this second aspect of the invention are largely analogous to the corresponding steps described above in connection with the first aspect of the invention. Embodiments mentioned in relation to these steps in the first aspect of the invention are largely compatible for the corresponding steps in the second aspect of the invention, of which some are exemplified below (typically without repeating the advantageous effects).
For example, the step of treating the SO2 gas stream with an alkaline solution may be performed in an SO2 scrubber, and the method may comprise the step of separation of the pretreated biomass slurry to remove a liquid fraction. Moreover, the method may comprise a steam explosion step, preferably arranged downstream of the reactor vessel. Additionally or alternatively, the method may comprise subjecting the fermentable sugars of the hydrolysate to fermentation in an aqueous liquid utilizing at least one fermenting microorganism under conditions in which at least a part of the fermentable sugars is fermented into a primary target chemical. Such fermentation may e.g. be carried out in a fermentation unit or fermentation vessel.
By treating the sulfite/bisulfite solution to form a separated gas stream and using the separated gas stream in at least one of process i) and ii), the SO2 added to the process can be re-used as a gas. Hereby, an efficient but yet simple way of re-using the SO2 from the process is provided. Besides the advantageous effects presented below for each one of the process i) and ii), by re-using at least SO2, a cost-effective process is provided. Moreover, by re-using at least SO2 from the process, required cleaning and removal of SO2 e.g. due to emission restrictions, can be reduced or even omitted. Moreover, by treating the SO2 gas stream with an alkaline solution to provide a sulfite/bisulfite solution and subsequently treating the sulfite/bisulfite solution to form a separated gas stream, the SO2 gas can be concentrated to a desired level before being used in at least one of process i) and ii). Thus, an increased control of the process is achieved.
By treating the sulfite/bisulfite solution to form a separated gas stream and using the separated gas stream in at least one of process i) and ii), e.g. both of process i) and i), a flexible and versatile way of re-using SO2 from the process is provided. That is, by providing a separated gas stream from the sulfite/bisulfite solution which may be used for different purposes in the process depending on the need, and using the separated gas stream in at least one of process i) and ii), a flexible and versatile way of re-using at least some substance from the process are provided.
According to at least one example embodiment, the steps of: retrieving gaseous SO2 from the pretreatment arrangement to provide an SO2 gas stream; treating the SO2 gas stream with an alkaline solution to provide a sulfite/bisulfite solution; treating the sulfite/bisulfite solution to form a separated gas stream; and using the separated gas stream in at least one of the processes i) and ii) are performed subsequently in the order as presented.
In accordance with the process i) the gaseous SO2 can be used to impregnate the lignocellulosic biomass material in the pretreatment arrangement, and thus externally provided SO2 can be reduced or even omitted.
In accordance with the process ii) the gaseous SO2 can be cooled to form an SO2 liquid stream, which advantageously can be used for various purposes, e.g. in accordance with the first aspect of the invention, and in particular to at least one of options a)-d).
According to at least one example embodiment, the step of treating the sulfite/bisulfite solution to form a separated gas stream comprises lowering the pH of the sulfite/bisulfite solution to reduce the solubility of SO2 in the solution.
Hereby, the gaseous SO2 may more easily be separate from the solution.
The method may further comprise the step of separating at least gaseous SO2 from the sulfite/bisulfite solution to form the separated gas stream, preferably by using heat.
Hereby, a simple but yet effective means for creating the separated gas stream is provided. For example, steam may be used to heat the sulfite/bisulfite solution.
The method may further comprise the step of recirculating the SO2 liquid stream into the pretreatment, hydrolyzing and/or fermentation step.
According to at least a third aspect of the invention, a system for treatment of lignocellulosic biomass is provided. The system comprises:
Such system may be used to carry out the method in accordance with both the first and second aspect of the invention. Thus, effects and features of this third aspect of the invention are largely analogous to those described above in connection with the first and second aspects of the invention. Embodiments mentioned in relation to the first and second aspects of the invention are largely compatible with the third aspect of the invention, of which some are exemplified below (typically without repeating the advantageous effects).
According to at least one example embodiment, the SO2 treatment unit comprises an inlet for receiving the alkaline solution, and/or an outlet for discharging the sulfite/bisulfite solution from the SO2 treatment unit.
According to at least one example embodiment, the pretreatment arrangement comprises an impregnation vessel configured to treat the lignocellulosic biomass with SO2, and a reactor vessel configured to subject the SO2 impregnated biomass from the impregnating vessel to an elevated temperature and pressure to provide said pretreated biomass slurry.
Hereby, an effective way of pretreating the lignocellulosic biomass is provided.
According to at least one example embodiment, the system further comprises a recirculation arrangement configured to supply at least a part of the sulfite/bisulfite solution to at least one of:
Effects, features and embodiments of this recirculation arrangement are largely analogous to those described above in connection with the method steps according to options a)-d) in accordance with the first aspect of the invention. The recirculation arrangement may e.g. comprise transport piping, applicable valves and tanks/reservoirs and corresponding control means. Thus, according to at least one example embodiment, the recirculation arrangement comprises a transportation pipe for supplying at least a part of the sulfite/bisulfite solution to at least one of options a)-d), and a pump configured to move a liquid, such as the sulfite/bisulfite solution, in the transportation line. The transportation line is typically arranged between the process equipment treating the SO2 gas stream with an alkaline solution to provide the sulfite/bisulfite solution (e.g. a scrubber) and at least on point in the process corresponding to at least one of options a)-d). Additionally, one or more valves for handling liquids, such as the sulfite/bisulfite solutions, is arranged along the transportation line.
According to at least one example embodiment, the system further comprises:
It should be noted that the system may comprise both the gas recirculation arrangement and the condenser. Effects, features and embodiments of the gas recirculation arrangement and the condenser are largely analogous to those described above in connection with the method steps according to process i) and ii) in accordance with the second aspect of the invention. The gas recirculation arrangement may e.g. comprise transport piping, applicable valves and tanks/reservoirs and corresponding control means. Thus, according to at least one example embodiment, the gas recirculation arrangement comprises a transportation pipe for supplying the separated gas stream to the impregnation vessel of the pretreatment arrangement to pretreat the lignocellulosic biomass material with SO2 present in the separated gas stream by means of and a compressor configured to move a gas, such as the separated gas stream, in the transportation pipe. The transportation pipe is typically arranged between the process equipment configured to treat the sulfite/bisulfate solution to form a separated gas stream and at least the impregnation vessel of the pretreatment arrangement. Additionally, one or more valves for handling gases, such as the separated gas stream, is arranged along the transportation pipe.
According to at least one example embodiment, the system further comprises a steam explosion configuration arranged downstream, or in an outlet region of, the reactor vessel.
According to at least one example embodiment, the system further comprises a fermentation unit arranged in fluid communication with and downstream of said hydrolysis unit, the fermentation unit being configured to subject the fermentable sugars of the hydrolysate to fermentation in an aqueous liquid utilizing at least one fermenting microorganism under conditions in which at least a part of the fermentable sugars are fermented into a primary target chemical.
The primary target chemical may e.g. be ethanol.
According to at least one example embodiment, the system comprises a control unit configured to perform at least one of the method steps of the first and/or second aspect of the invention. For example, the system may comprise additional units and components known to those skilled in the art. For example, a separation unit may be arranged between the pretreatment arrangement and the hydrolysis unit, and/or between the hydrolysis unit and the fermentation unit.
It should be understood that the wording “process” in the application text generally indicates the process from providing a lignocellulosic biomass material prior to subjecting it to the pretreatment (or alternatively from the step pretreating a lignocellulosic biomass material in a pretreatment arrangement) to discharging the pretreated biomass slurry from the reactor vessel, or discharging the hydrolysate from the hydrolysis unit or discharging the primary target chemical from the fermentation step.
The various aspects of the present invention, including its particular features and advantages, will be readily understood from the following detailed description and the accompanying drawings, in which:
The present invention will now be described more fully hereinafter with reference to the accompanying drawings. The present invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein; rather, these embodiments are provided for thoroughness and completeness, and fully convey the scope of the present invention to the skilled person.
In the embodiment of
The lignocellulosic biomass may be, but is not limited to, hardwoods, softwoods, sugarcane bagasse, energy cane, corn stover, corn cobs, corn fibers, straw from rice, wheat, rye and other crop or forestry residues. As illustrated by the arrow 95, steam and/or additional catalysts may in embodiments be added to the reactor vessel 140 for certain pretreatment conditions.
The pretreatment arrangement 100 further comprises an SO2 injection arrangement 130 configured to supply an SO2 feed 90 to the lignocellulosic biomass in the impregnation vessel 120. The SO2 injection arrangement 130 may include a controllable valve (not shown) having an adjustable opening configuration for varying the SO2 feed. Typically, the SO2 injection arrangement 130 is configured to supply the SO2 to the impregnation vessel 120 in gaseous form, but a configuration in which the SO2 is fed to the impregnation vessel 120 as a liquid is within the scope of the invention.
In short, the pretreatment arrangement 100 operates as follows. The lignocellulosic biomass material 80 enters the pretreatment arrangement 100, and the impregnation vessel 120, via the upstream inlet 122. In the impregnation vessel 120, the lignocellulosic biomass is treated or impregnated with SO2 by the use of the SO2 injection arrangement 130. The operating temperature of the impregnation vessel 120 may e.g. be in the range of 20° C. to 90° C., e.g. between 20° C. to 60° C. Subsequently, the SO2 impregnated biomass from the impregnation vessel 120 is fed to the reactor vessel 140. In the reactor vessel 140, and during operation, the SO2 impregnated biomass from the impregnation vessel 120 is subject to an elevated temperature and pressure forming a biomass slurry. For example, the temperature in the reactor vessel 140 during pretreatment may be in the interval of 185° C. to 225° C., such as 200° C. to 215° C., and the pressure in the interval of 10 to 25 bar, such as 15 to 20 bar. The reactor vessel 140 may according to one example embodiment be a vertical reactor vessel. However, horizontal, as well as inclined, reactor vessels are also conceivable for the purpose of the present disclosure. The pretreatment arrangement 100 may further comprise specific types of inlets (such as e.g. an inlet hopper), feeding means (e.g. a plug screw feeder) for transporting the biomass material internally of the pretreatment arrangement 100, and moisture adjusting units (e.g. compressing, dewatering units) known to those skilled in the art.
The hydrolysis unit 200 is arranged in fluid communication with, and downstream of, the pretreatment arrangement 100. The hydrolysis unit 200 is configured to hydrolyze the pretreated biomass slurry 82 with at least one aqueous hydrolyzing liquid comprising saccharification enzymes, under conditions in which at least a part of the pretreated biomass slurry is hydrolyzed to a hydrolysate 84. The hydrolysate 84 comprises fermentable sugars and inhibitory substances.
The fermentation unit 300 is arranged in fluid communication with, and downstream of, the hydrolysis unit 200. The fermentation unit is configured to subject the fermentable sugars of the hydrolysate to fermentation in an aqueous liquid utilizing at least one fermenting microorganism under conditions in which at least a part of the fermentable sugars is fermented into a primary target chemical 86. The primary target chemical can e.g. be ethanol.
The system 1000 in
The system 1000 in
In addition to, or as an alternative to, the recirculation arrangement 600, the system 100 may comprise a sulfite/bisulfite treatment unit 700 configured to treat the sulfite/bisulfite solution to form a separated gas stream 98. The sulfite/bisulfite treatment unit 700 may e.g. comprise a flash tank, or other separating unit, in which heat (e.g. steam) is used to cause a separation of gaseous substances from the sulfite/bisulfite solution 97. For example, the amount of SO2 in the separated gas stream 98 can be increased by reducing the pH of the sulfite/bisulfite solution 97 prior to, or in, the sulfite/bisulfite treatment unit 700. Hereby, the solubility of SO2 in the sulfite/bisulfite solution 97 is reduced, thereby facilitating gaseous removal of the same.
The system 1000 may further comprise a gas recirculation arrangement 800 arranged downstream of the sulfite/bisulfite treatment unit 700. The gas recirculation arrangement 800 is configured to supply the separated gas stream 98 back to the pretreatment arrangement 100, and here specifically to the impregnation vessel 120. Hereby, the SO2 in the separated gas stream 98 can be used to pretreat the lignocellulosic biomass material. Additionally, or alternatively, the separated gas stream 98 can be directed to a condenser 900 configured to cool the separated gas stream 98 to form an SO2 liquid stream 99. Hereby, the SO2 will furthermore be separated from other gaseous substance(s) present in the separated gas stream 98. The SO2 liquid stream 99 can e.g. be recirculated into the system 1000 via the recirculation arrangement 600 according to at least one of options a)-d) previously described.
The system 1000 may also comprise a product recovery unit, such as distillation or ion exchange chromatography, arranged downstream of and in fluid communication with the fermentation unit 300.
An embodiment of the invention will now be described with reference to the flow chart presented in
First, the main steps, and significant optional steps of the method are described, where after further optional steps are presented. In step S10, a lignocellulosic biomass material is pretreated in a pretreatment arrangement (e.g. pretreatment arrangement 100 in
In an optional step S20, the pretreated biomass slurry is hydrolysed in a hydrolysis unit (e.g. the hydrolysis unit 200 in
In an optional step S30 the fermentable sugars of the hydrolysate is subject to fermentation in an aqueous liquid utilizing at least one fermenting microorganism under conditions in which at least a part of the fermentable sugars are fermented into a primary target chemical, e.g. ethanol (e.g. by utilizing the fermentation unit 300 in
It should be noted that step S20 and step S30 are optional and that the following steps of the method can be carried out based on the pretreated biomass slurry from the pretreatment arrangement.
In step S40, gaseous SO2 is retrieved from the pretreatment arrangement to provide an SO2 gas stream (e.g. by utilizing the retrieving arrangement 400 in
In a step S50, the SO2 gas stream from step S40 is treated with an alkaline solution to provide a sulfite/bisulfite solution (e.g. by utilizing the SO2 treatment unit 500 in
In step S60, at least a part of the sulfite/bisulfite solution from step S50 is supplied to the process (e.g. by utilizing the recirculation arrangement 600 in
In sub-step S60a, the sulfite/bisulfite solution is supplied to the lignocellulosic biomass material prior to pretreating the lignocellulosic biomass material in the pretreatment arrangement, i.e. prior to step S10. As mentioned in relation to
In sub-step S60b, the sulfite/bisulfite solution is supplied to the lignocellulosic biomass material in the pretreatment arrangement, e.g. supplied to the reactor vessel. Thus, the sulfite/bisulfite solution may be used during the pretreatment step S10. As mentioned in relation to
In sub-step S60c, the sulfite/bisulfite solution is supplied to the pretreated biomass slurry discharged from the reactor vessel, i.e. subsequent to step S10 but prior step S20 (i.e. prior to subjecting the pretreated biomass slurry to at least one aqueous hydrolysing liquid). That is, the sub-step S60c may be performed by supplying the sulfite/bisulfite solution to a process location downstream the reactor vessel, e.g. between the reactor vessel and the hydrolysing unit. As mentioned in relation to
In sub-step S60d, the sulfite/bisulfite solution is supplied to the fermentable sugars of the hydrolysate, i.e. subsequent to step S20, and possibly prior to, or during, step S30 (i.e. either prior to, or during the fermentation step). As mentioned in relation to
It should be understood that at least one of the sub-steps S60a-S60d are used in the method to supply the sulfite/bisulfite solution to the process. However, use of more than one of the sub-steps S60a-S60d, and/or other options of supplying the sulfite/bisulfite solution to the process, are within the scope of the invention.
In the following, further optional steps of the method are described, although they are not explicitly stated as optional.
In a step S10c, the biomass slurry is subject to a steam explosion, preferably arranged downstream, or in an end section of, the pretreatment arrangement or reactor vessel.
In a step S14 the pretreated biomass slurry is subject to a separation in order to remove a liquid fraction. For example, the liquid fraction is removed from the process, and the solid fraction are further used in the downstream process (as step S20 and step S30).
In a step S62 the hydrolysate is detoxified by decreasing the concentration of at least one of the inhibitory substances using the sulfite/bisulfite solution. The inhibitory substances are typically still present in the hydrolysate, but may undergo reactions resulting in less toxic states with regards to yeast and/or other enzymes used in downstream process steps. The step S62 may e.g. be embodied by sub-step S60c.
However, it should be noted that any upstream supply of the sulfite/bisulfite solution at least to some extent contributes to the advantageous effects of any downstream option of supply of the sulfite/bisulfite. For example, even if solely the sub-step S60a is utilized, the advantageous effects of sub-steps S60b, S60c and S60d, or step S62 of detoxification of the hydrolysate, are still to at least some degree met, as the substances of the sulfite/bisulfite solution are following the flow of biomass further downstream.
In a step S64, the pH of the pretreated biomass slurry is increase to between 4 and 6, or between 4.5 and 5.5, using the sulfite/bisulfite solution. The step S54 may e.g. be embodied by sub-step S60c, but as previously mentioned, also sub-steps S60a and/or sub-step S60b could be used to increase the pH of the pretreated biomass slurry as the substances causing the pH increase are following the flow of biomass further downstream.
An alternative embodiment of the invention will now be described with reference to the flow chart presented in
Many of the steps in
In a step S70 subsequent to step S50 of treating the SO2 gas stream from step S40 with an alkaline solution to provide a sulfite/bisulfite solution (e.g. by utilizing the SO2 treatment unit 500 in
In a step S80 subsequent to step S70, the separated gas stream is utilized in the process. The separated gas stream may be used in a process according at least one of the following sub-steps:
In sub-step S80a, the separated gas stream is used to pretreat the lignocellulosic biomass material with SO2 present in the separated gas stream, e.g. in the impregnation vessel of the pretreatment arrangement. That is, SO2 earlier supplied to the process is re-circulated to again pretreat the lignocellulosic biomass material (e.g. by utilizing the recirculation arrangement 800 in
In a sub-step S80b, the separated gas stream is cooled (e.g. in the condenser 900 of
The methods presented in
Turning back to
Even though the present disclosure has been described with reference to specific exemplifying embodiments thereof, many different alterations, modifications and the like will become apparent for those skilled in the art.
Variations to the disclosed embodiments can be understood and effected by the skilled addressee in practicing the present disclosure, from a study of the drawings, the disclosure, and the appended claims. Furthermore, in the claims, the word “comprising” does not exclude other elements or steps, and the indefinite article “a” or “an” does not exclude a plurality.
| Number | Date | Country | Kind |
|---|---|---|---|
| 20176288.7 | May 2020 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2021/063744 | 5/24/2021 | WO |
