Method for treating lignocellulosic biomass by impregnation
阅读说明：本技术 通过浸渍处理木质纤维素生物质的方法 (Method for treating lignocellulosic biomass by impregnation ) 是由 C·艾马尔 P-A·布永 R·鲁塞 O·卡尔诺 于 2018-12-04 设计创作，主要内容包括：本发明涉及一种通过酸性液体处理木质纤维素生物质以生产第二代(2G)糖汁的方法。这些糖汁可以用于通过生物化学途径生产其他产品(例如,醇,如乙醇、丁醇或其他分子,例如溶剂,如丙酮等)。该方法包括分析在该方法中取出的液体料流和调节浸渍液的组成以保持所述料流的酸性力恒定。(The present invention relates to a method for the treatment of lignocellulosic biomass by means of an acidic liquid to produce second generation (2G) sugar juice. These sugar juices can be used to produce other products (e.g., alcohols such as ethanol, butanol or other molecules, e.g., solvents such as acetone, etc.) by biochemical routes. The process comprises analyzing the liquid stream withdrawn in the process and adjusting the composition of the impregnation liquor to keep the acidity of said stream constant.)
1. A method for continuously processing lignocellulosic biomass to produce a sugar liquor, comprising the steps of:
a) impregnating the biomass with an impregnation solution having a pH of 0.1 to 7 by contacting the biomass with the impregnation solution,
b) separating the impregnated biomass obtained in step a) to produce wet biomass having a solids content of at least 15 wt% and a separated liquid,
c) pretreating the wet biomass obtained in step b) to produce a pretreated biomass, in the course of which one or more liquid streams are withdrawn,
characterized in that the method comprises
d) Analyzing the composition of the liquid separated from step b) and/or one or more liquid streams withdrawn during the pretreatment of the biomass, and
e) adjusting the composition of the impregnation liquor used in step a) to keep constant throughout the process the acidity of the liquor separated from step b) and/or the liquor stream withdrawn during biomass pretreatment, which acidity corresponds to the presence of H+The amount of ions.
2. The method according to the preceding claim, characterized in that the impregnation liquid comprises at least one acid and optionally water.
3. Method according to one of the preceding claims, characterized in that it comprises a step of preparing an impregnation liquid before the impregnation step a).
4. The method according to one of the preceding claims, characterized in that the impregnation step is carried out at a temperature of 10 to 95 ℃ and the residence time of the biomass in the impregnation step is 20 seconds to 12 hours.
5. Method according to one of the preceding claims, characterized in that the pH of the impregnation solution is between 0.1 and 6, preferably between 0.1 and 2.
6. Method according to one of the preceding claims, characterized in that the impregnation liquid is an aqueous solution of a strong acid, selected for example from sulfuric acid, hydrochloric acid and nitric acid, having an acid content of 0.5 to 8% by weight of acid relative to the total weight of the impregnation liquid.
7. The method according to one of the preceding claims, characterized in that the separation step can be carried out by draining, decanting, centrifuging or pressing the impregnated biomass.
8. The method according to one of the preceding claims, characterized in that the solids content of the wet biomass obtained in step b) is 25-70 wt. -%, preferably 40-65 wt. -%.
9. Method according to one of the preceding claims, characterized in that step c) of pre-treating the wet biomass is carried out by cooking, preferably by steam explosion.
10. The method according to one of the preceding claims, characterized in that step d) of analyzing the composition of the liquid separated from step b) and/or of one or more liquid streams withdrawn during biomass pretreatment comprises measuring the acidity of the liquid separated from step b) and/or of the liquid streams withdrawn during biomass pretreatment throughout the method.
11. Method according to the preceding claim, characterized in that the measurement of the acidity of the liquid and/or the liquid stream is carried out by measuring the pH or by measuring the conductivity, in particular continuously or at a given frequency.
12. The method according to one of the preceding claims, characterized in that the liquid stream withdrawn during biomass pretreatment is a liquid stream withdrawn downstream of the impregnation step a) and upstream of the subsequent biomass treatment step.
13. The method according to one of the preceding claims, characterized in that step e) of adjusting the composition of the impregnation liquor used in step a) is carried out by adding water and/or acid to the impregnation liquor in order to keep the acidity of the liquid separated from step b) and/or the liquid stream withdrawn during the biomass pretreatment constant, in particular within ± 20%, preferably within ± 10%, throughout the process.
14. The method according to one of the preceding claims, characterized in that the method comprises a step of recycling the liquid separated from step b), the liquid stream withdrawn during the biomass pretreatment and/or the liquid stream withdrawn during the subsequent biomass treatment step, for example by enzymatic hydrolysis and/or alcoholic fermentation, into the impregnation step a).
15. The method according to one of the preceding claims, characterized in that the method comprises a step of treating at least a part of the pretreated biomass by enzymatic hydrolysis after the pretreatment step c) to produce the sugar liquor.
16. Method according to one of the preceding claims, characterized in that at least a part of the sugar liquor is subjected to alcoholic fermentation.
Technical Field
The present invention relates to a process for the treatment of lignocellulosic biomass by means of an acidic liquid to produce a "second generation" (2G) sugar liquor. These sugar solutions can be used to produce other products (e.g., alcohols such as ethanol, butanol, or other molecules, e.g., solvents such as acetone, etc.) by biochemical routes. The process comprises analyzing the liquid stream withdrawn in the process and adjusting the composition of the impregnation liquor to keep the acidity power (acid power) of said stream constant.
Prior Art
Lignocellulosic biomass represents one of the most abundant renewable resources on earth. The bases (substrates) considered are very diverse and they relate to both wood bases such as various woods (hardwood and softwood), byproducts derived from agriculture (wheat straw, corn cobs, etc.) or other agricultural products, paper, etc., industries.
The process for biochemical conversion of lignocellulosic material to 2G sugar liquor comprises in particular a pretreatment step and a step of hydrolysis with an enzyme mixture. These methods also typically include an impregnation step prior to pretreatment. The sugar liquor produced by enzymatic hydrolysis is then processed, for example by fermentation, and the process further comprises a separation step and/or a step of purifying the end product.
Lignocellulosic biomass is composed of three main polymers: cellulose (35% to 50%), which is a polysaccharide consisting essentially of hexoses; hemicellulose (20% to 30%), which is a polysaccharide consisting essentially of pentoses and hexoses; and lignin (15% -25%), which is a structurally complex and high molecular weight polymer consisting of aromatic alcohols linked by ether linkages. These different molecules result in a variety of inherent properties of the plant wall and organize themselves into complex tangles (entanglements). In addition to these three main compounds, lignocellulosic biomass also contains significant acetyl groups and ash. This "ash" consists of the following minerals: silicon dioxide, compounds containing calcium, magnesium, sodium, potassium, phosphorus and/or aluminum. Their content and their composition vary widely from one type of biomass to another (straw vs. wood, etc.) and with soil climate (climate) culture conditions and harvest conditions. Different batches of straw will have different properties with different amounts of ash. For example, a Method for quantifying the Ash content of lignocellulosic products is described in the Standard ASTM E1755 "Standard Test Method for Ash in Biomass".
Among the three basic polymers that make up lignocellulosic biomass, cellulose and hemicellulose are those capable of producing 2G sugar liquors.
Typically, hemicellulose is mainly broken down into sugars during pretreatment, while cellulose is converted to glucose by enzymatic hydrolysis. However, the crude cellulose is still inaccessible to enzymes and thus requires pretreatment. This pretreatment makes it possible to modify the physicochemical properties of the lignocellulosic material in order to improve the accessibility of the cellulose to the enzymes and its reactivity towards enzymatic hydrolysis.
One of the most effective pretreatments is acid steam explosion, which enables almost complete hydrolysis of hemicellulose and significantly improves the accessibility and reactivity of cellulose to enzymes. Such pre-treatment may be preceded by other treatments.
Patents US-8057639 and US-8512512 propose a process comprising a first step of hydrolysis of hemicelluloses into C5 sugars under mild conditions to protect them from degradation. This step is carried out in a first reactor at a pressure of 1.5 bar or more by injecting steam, at a temperature of 110 ℃ or more and optionally in the presence of a weak acid. After this step, washing is carried out to extract and recover the C5 sugar juice, and then the remaining biomass, rich in cellulose and lignin, is sent to the second step (second reactor), where steam explosion takes place. This second reactor is operated at a higher pressure than the first reactor, wherein high pressure steam is injected, which results in a sudden expansion of the biomass (steam explosion).
Patent application US-2012/0104313 also proposes a treatment step by contacting the biomass with water or steam at 100-210 ℃ for 1 minute-24 hours before the steam explosion. After separation of the hemicellulose-rich liquid phase, the solid is then transferred to a steam explosion step.
Patent EP2610346 describes a process for treating lignocellulosic biomass in four steps: treatment in a liquid at a temperature of 100-150 ℃, followed by separation of the liquid/solid, followed by pretreatment of the obtained solid fraction in the presence of water or steam at a temperature of 100-210 ℃ for a period of 1 minute to 24 hours, and finally liquid/solid separation.
In the context of their research, the applicant has demonstrated that it is possible to improve the performance of known biomass pretreatment processes more significantly. In particular, the presence of ash and acetyl groups in biomass in variable amounts tends to change its properties. However, measuring ash content and determining acetyl groups is expensive in terms of time and difficult to implement to enable continuous monitoring of the process.
Thus, the applicant has found that by adjusting the composition of the impregnation liquor as a function of the acidity of the liquid stream obtained from the biomass pretreatment process (the liquid separated after impregnation and/or any one liquid stream withdrawn during the biomass pretreatment), the performance and stability of the biomass treatment process can be significantly improved. Thus, in fact, by adjusting in real time the composition of the impregnation liquor used, it is possible to counteract the inherent variability of the biomass and to ensure the stability of the downstream performances, in particular in terms of reactivity of the biomass treated with cellulases.
Disclosure of Invention
The present invention therefore proposes a process for the continuous treatment of lignocellulosic biomass to produce a sugar liquor, comprising the following steps:
a) impregnating the biomass with an impregnation solution having a pH of 0.1 to 7 by contacting the biomass with the impregnation solution,
b) separating the impregnated biomass obtained in step a) to produce wet biomass having a solids content of at least 15 wt% and a separated liquid,
c) pretreating the wet biomass obtained in step b) to produce a pretreated biomass, in the course of which one or more liquid streams are withdrawn,
characterized in that the method comprises
d) Analyzing the composition of the liquid separated from step b) and/or one or more liquid streams withdrawn during the pretreatment of the biomass, and
e) the composition of the impregnation liquor used in step a) is adjusted to keep the acidity of the liquor separated in step b) and/or the liquor stream withdrawn during biomass pretreatment constant throughout the process.
For the purposes of the present patent application, the term "sugar liquor" means any aqueous mixture of sugars obtained from lignocellulose, such as glucose, xylose, mannose, galactose and arabinose.
Indeed, applicants' credit demonstrates that inherent variations in biomass composition can be compensated to ensure that the treated biomass always has substantially the same level of reactivity to cellulases. In fact, applicants have found that by controlling the acidity of certain liquid streams produced in the process, and by adjusting the composition of the acidic impregnation liquor to keep the acidity constant, the biomass treatment process can be adjusted despite its inherent compositional variations.
In the context of the present invention, the abbreviation "SC" denotes the solids content of Biomass, which can be measured in particular according to the Standard ASTM E1756-08(2015), "Standard Test Method for Determination of Total solid sin biomas".
Detailed Description
The process according to the invention is a continuous process for treating lignocellulosic biomass prior to enzymatic hydrolysis.
It is integrated into processes involving the production of second generation sugars from which many biochemical pathways enable oxygen-containing molecules (e.g. alcohols such as ethanol, butanol, etc.) to be obtained.
The process is compatible with processes for producing 2G sugars (i.e., those obtained from lignocellulosic biomass) or more broadly bio-based molecules (i.e., molecules derived from or derived from natural base stocks).
Biomass
The method according to the invention proposes a continuous treatment of lignocellulosic biomass.
The biomass may be derived from a variety of sources, such as woody bases, such as various woods (hardwood and softwood), from agriculture (wheat straw, corn cobs, etc.), or from other by-products of agricultural, paper, and like industries.
Depending on the biomass used (straw, wood, etc.), before its use in the process of the invention, a milling step can be envisaged to obtain a particle size compatible with the technical means and operating conditions of the steps of the process. For this reason, simple cutting may be sufficient, but milling with or without refining may be required.
Typically, the biomass used in step a) of the process of the invention has a particle size (largest dimension) of not more than 300 mm. Typically, the grinding of the straw is carried out with a 5-100 mm screen and the wood is cut into parallelepipedal slices having a length of 20-160 mm, a width of 10-100mm and a thickness of 2-20 mm.
The biomass is preferably conveyed to the impregnation step via the first transfer zone. According to a particular embodiment, the transfer zone and the impregnation zone may be separated by a biomass plug (bioglass plug) which prevents the backflow of liquid from said first zone back to the transfer zone or even further upstream.
Preparation of the impregnation liquid
The impregnation liquor used in the process of the present invention is preferably an acidic liquor comprising at least one acid and optionally water.
In particular, some biomasses have a very low solids content (e.g. less than 50% SC) and therefore the water content is high enough that it is not necessary to add more water for impregnation. In this case, the impregnation liquor is prepared by introducing only the acid which will be mixed with the water already present in the biomass during the impregnation step.
In particular, the pH of the acidic liquid is from 0.1 to 7.0, preferably from 0.1 to 6, preferably from 0.1 to 2.
According to a preferred embodiment, the liquid comprises at least one acid and water.
Preferably, the acidic liquid is an aqueous solution of a strong acid, for example selected from sulfuric acid, hydrochloric acid and nitric acid, the acid content being between 0.5 and 8% by weight of acid relative to the total weight of the liquid. According to a preferred embodiment, the impregnation solution is a sulfuric acid solution.
Liquids of this type are well known to those skilled in the art and any acid commonly used for impregnation is suitable for use. The amount of acid and the temperature of the liquid are generally fixed. Methods of obtaining and maintaining temperature are known to those skilled in the art.
The method according to the invention may comprise a step of preparing the impregnation solution prior to the impregnation step a).
In this step, the impregnation solution is preferably heated to a temperature of 10 to 95 ℃. This step may be carried out in a liquid preparation zone located upstream of the impregnation zone.
Various devices may be used, such as a mixing tank or a mixer (preferably a static mixer) equipped with a stirring system. Preferably, the device is equipped with sensors for measuring the pH and flow rate of the water, acid and recycled liquid. All of these sensors allow control of the equilibrium flow rate and acidity for stable continuous operation under desired conditions.
The liquid preparation device may be equipped to allow heating of its contents, for example by means of a jacket, coils and/or exchangers located on a recirculation loop (described below) close to or directly on the device (tank, mixer, etc.). The device for preparing the liquid may be connected to the impregnator, in particular by one or more pipes conveying the liquid.
Thus, the liquid can be prepared in a suitable concentration and at a suitable flow rate, which makes it possible to obtain the required acidity power for the liquid stream withdrawn downstream of the impregnation.
Liquid preparation is also a step in which the operating parameters, such as temperature, pH or any other characteristic, can be adjusted. The appropriate acid concentration is adjusted by the input of acid and/or water.
Step of impregnation
The method of the invention comprises a step a) -impregnating the biomass with an impregnation solution having a pH of 0.1-7 by contacting the biomass with the impregnation solution.
Preferably, in the method according to the invention, the impregnation step is carried out at a temperature in the range of 10 to 95 ℃ and the residence time of the biomass in said impregnation step is 20 seconds to 12 hours. Preferably, the residence time of the biomass is from 30 seconds to 60 minutes. The impregnation step is preferably carried out at atmospheric pressure.
The impregnation step is carried out by contacting the biomass with an impregnation solution. This contacting may be performed by, for example, dipping or spraying. During the impregnation process, it is generally preferred to keep the liquid level substantially constant by providing an impregnation liquid.
The impregnation step may be carried out in a batch or continuous mode. Preferably, this step is carried out in a continuous mode. The impregnation may be carried out in one or more impregnation reactors, preferably in a single impregnation reactor.
The impregnation step is carried out in apparatuses known to the person skilled in the art, for example in stirred reactors, by horizontal or vertical passage of the biomass in a liquid bed (throughput), by spraying on a belt conveying the biomass or in a conveying screw.
The impregnation reactor (or impregnator) is typically equipped with one or more tools that transfer the lignocellulosic biomass from its inlet to the outlet orifice. These means may be, for example, a spiral or a belt. The impregnator is also equipped with one or more conduits for conveying acid, water or acidic liquid and, optionally, one or more conduits for withdrawing acidic liquid.
According to a preferred embodiment, the biomass impregnated with liquid may be discharged during impregnation to extract at least some of the acidic liquid before being sent to the separation step b). In this embodiment, the solids content of the discharged biomass is from 10 to 40% by weight, preferably from 15 to 30% by weight.
The impregnation reactor (impregnator) may be equipped with one or more pipes for transporting the impregnation liquid when it is prepared in the preceding step, and one or more pipes for introducing water and/or acid and for removing liquid.
According to a very particular embodiment, the impregnation step can be carried out in a tubular impregnation reactor (or impregnator) which is vertical or inclined at an angle of less than 60 ° with respect to the vertical. The reactor comprises in particular two overlapping impregnation zones preferably located on the same axis. The bottom zone is referred to as the first impregnation zone and receives the pressed biomass obtained from the first transfer zone through an orifice. The upper zone (top zone) is referred to as the second impregnation zone and it receives the wet, discharged biomass originating from the first impregnation zone. In this embodiment, the impregnation reactor (impregnator) may be equipped with one or more conveying screws which transfer the biomass via the bottom of the first impregnation zone to the outlet orifice via the top of the second impregnation zone. The first impregnation zone (thus the area where impregnation of the biomass with the impregnation liquid takes place) corresponds to the space filled with the impregnation liquid. The second impregnation zone does not in particular contain any continuous liquid phase. It is particularly advantageous to maintain a constant distribution between the first impregnation zone and the second impregnation zone. For this purpose, the reactor is equipped with a detection system (level sensor), preferably with a system for regulating the level, which makes it possible to ensure filling to the desired level. The effect of compressing the biomass during the formation of the plug (at the conveyor screw that conveys the biomass to the impregnation step) and the effect of decompressing at the inlet of the first impregnation zone filled with liquid make it possible to better saturate the biomass (sponge effect). The biomass is transferred through a first zone in which it is impregnated towards a second impregnation zone located above the liquid surface. In the second impregnation zone, a part of the impregnation liquor is separated from the impregnated biomass by draining during the ascent into the second impregnation zone, the drained liquor being extracted from the second impregnation zone for recycling. Preferably, the second impregnation zone is equipped with a screen to hold the wet biomass in the second impregnation zone, whereby the screen allows the drained liquid to flow from the second impregnation zone into the first impregnation zone.
Warp beamSeparation step of impregnated biomass
At the end of the impregnation step a), the process according to the invention comprises a step b) -separating the impregnated biomass obtained in step a) to produce a wet biomass having a solids content of at least 15% by weight and a separated liquid.
The separation step may be performed by any technique known to the person skilled in the art, for example by draining, decanting, centrifuging or pressing the impregnated biomass, or a combination of these techniques. According to a preferred embodiment, the separation is performed by pressing.
In particular, the separation step b) may comprise discharging the wet biomass to reach a solids content of 10 to 40 wt. -%, followed by a second separation, for example by pressing, to reach a higher solids content of 40 to 70 wt. -%. This embodiment is particularly preferred when no draining is performed during the impregnation step a).
Preferably, at the end of the separation step b), the wet biomass has a solids content of from 25% to 70% by weight and preferably from 40% to 65% by weight.
In a particular embodiment of the invention, the pressing of the wet biomass may be carried out simultaneously with its transfer to the pretreatment step c), in particular when said step comprises a cooking process described below. Such an implementation of the separation step b) is for example carried out by means of a screw known to the person skilled in the art as a plug screw feeder (plug screw feeder). The spiral has a tapered portion that is connected to the inlet of the pretreatment reactor. At the end of the conical section, just before entering the inlet of the pretreatment reactor, a plug of biomass is formed. The formation of the pressed lignocellulosic biomass plugs ensures the pressure tightness of the cooking reactor that can be used in the pretreatment step c). The conveyor screw may also be equipped with one or more pipes for taking off waste liquid separated during the pressing process, called pressing liquid.
During the process of the invention, the spent steeping liquor is substantially extracted, so that the solids content of the biomass can be significantly increased for its subsequent treatment and its conversion into sugars. The production of biomass with a high solids content may allow energy savings for heating the medium to the desired pretreatment temperature and make it possible to obtain pretreated biomass also with a high solids content SC. Thus, the transportation of the pretreated biomass to the subsequent enzymatic hydrolysis step is facilitated and the enzymatic hydrolysis of biomass with high SC makes it possible to obtain concentrated (hydrolysed) sugar solutions, making it possible to target high fermentation titers (alcohol content) and thus to reduce the costs associated with the separation step (in particular by distillation) for the beneficial utilization of these alcohols. Furthermore, performing the process while maintaining a high biomass solids content makes it possible to reduce the volume of the fermentation (and hydrolysis) tank and reduce the amount of wastewater produced by the process.
The separation zone used in step b) can be equipped in particular with a pipe for withdrawing the resulting waste liquid (called press liquid) separated from the wet biomass.
Step of pretreatment
The process of the invention further comprises a step c) -pretreating the wet biomass obtained in step b) to produce a pretreated biomass, in the course of which one or more liquid streams are withdrawn.
The pretreatment in particular relates to changing the physical and physicochemical properties of the cellulose fraction, such as its degree of polymerization and its crystalline state. In particular, the pretreatment involves hydrolyzing the hemicellulose present in the biomass and allowing the cellulose to better access the enzymes.
According to a preferred embodiment, step c) of pretreating the wet biomass is carried out by cooking, preferably by steam explosion.
For example, the cooking is carried out in a cooking zone operating at a pressure of 0.1 to 4 MPa at a temperature of 100 ℃ to 250 ℃, more preferably 130 ℃ to 230 ℃. The residence time of the biomass in the cooking zone is from 10 seconds to 4 hours, more preferably from 3 minutes to 1 hour.
Cooking may be carried out in a batch or continuous manner. It can be carried out in any apparatus known to the person skilled in the art, for example stirred reactors, horizontal tubular reactors equipped with a conveyor screw, unstirred batch reactors, etc. The thermal energy required for cooking can be supplied by heat exchange with a heat transfer fluid (indirect), by electrical heating or by direct injection of a hot fluid such as pressurized water or steam.
At the end of the cooking, the discharge of the pretreated biomass can be carried out by rapid depressurization, by slow depressurization, after a temperature reduction by direct or indirect heat exchange or the like.
In a preferred embodiment, the process is referred to as steam explosion (or "steam explosion"), by heating the cooking zone with steam by direct injection, followed by sudden decompression of the medium. This is a method of rapidly bringing lignocellulosic biomass to high temperatures by injecting pressurized steam. The stopping of the process occurs by sudden decompression.
The operating conditions of the steam explosion method can be notably as follows:
steam is directly injected into the reactor;
the temperature of the reactor is typically 150 ℃ to 250 ℃, preferably 160 ℃ to 220 ℃,
a pressure of 0.5 to 2.5 MPa, more preferably 0.8 to 2.0 MPa,
the residence time before the expansion stage is from 10 seconds to 25 minutes, preferably from 3 minutes to 15 minutes.
The steam explosion may be performed in a batch or continuous mode, and the depressurization step to allow deconstruction of the biomass may be performed in one or more steps.
During the pretreatment step, various liquid streams may be withdrawn. These are in particular hot fluids (liquids or vapours) injected for the pre-treatment, such as pressurized water or steam.
The recovered vapor is advantageously recycled to the vapor explosion step after compression, or optionally to an on-site facility.
According to a particular embodiment, the pre-treatment step may be carried out in a horizontal tubular reactor (i.e. a reactor that may be very slightly inclined for liquid flow), for example equipped with a spiral for transferring the biomass through the continuous zone. The screw ensures continuous transport of the biomass, the speed of the screw being adjusted to meet the residence time conditions. At the end of the helix (at the end of the reactor), the biomass is very rapidly entrained by the steam to an expansion zone in a line called a lance tube (blowline) which has a reduced diameter relative to the cooking zone. The expansion zone comprises a line in which the biomass circulates and passes through a cross-sectional restriction member (cross-section restriction member) and then undergoes a sudden expansion after the restriction is cleared. The blowing tube has a cross-sectional limiting member which may be an orifice allowing a small flow area or a valve with an adjustable aperture (e.g. a diaphragm valve). Under this limit, the biomass arrives at very high transport speeds and undergoes rapid and large pressure changes, then expands suddenly after clearing the limit, which deconstructs the cooked biomass. That is why it is called a steam explosion. Once through the expansion zone, the steam entrains the biomass through the remainder of the injection tube, which has a larger diameter than the restriction (or which regains its diameter upstream of the restriction), which conveys the biomass to a zone for separation of the steam, for example through a cyclone.
The pretreated biomass obtained from step c) now has sufficient accessibility of the cellulose to the enzymes for treatment by enzymatic hydrolysis for the production of 2G sugars.
Analyzing the flow of the material flow and adjusting the composition of the impregnation solution
The inventive method is characterized in that it comprises a step d) -analyzing the composition of the liquid separated off in step b) and/or of one or more liquid streams removed during the pretreatment of the biomass.
In particular, the liquid stream withdrawn during the biomass pretreatment is a liquid stream withdrawn downstream of the impregnation step a) and upstream of the subsequent biomass treatment step, in particular upstream of the cooking step.
According to a preferred embodiment, step d) comprises analyzing the composition of the liquid separated from step b), called the pressing liquid.
In particular, the applicant's credit demonstrates that controlling the composition, in particular the acidity, of the liquid separated from step b) and/or of the liquid stream or streams withdrawn during the pretreatment of the biomass makes it possible to balance the inherent variability of the biomass and to ensure the stability of the downstream performances, in particular in terms of reactivity of the biomass treated with cellulases.
In particular, the analysis of the composition of the liquid separated from step b) and/or of the liquid stream or streams withdrawn during the pretreatment comprises measuring the acidity of the liquid separated from step b) and/or of the liquid stream withdrawn during the pretreatment of the biomass throughout the process, preferably by measuring the pH of the liquid and/or of the liquid stream, the measurement being in particular carried out continuously or at a given frequency.
Acidity is defined as the H present in the liquid under consideration+The amount of ions. It can be measured by various parameters by methods known to those skilled in the art. For example, the acidity force can be measured by a titration analysis method (monitoring a change in pH during stepwise addition of an alkali solution), by measuring the pH of a solution and/or by measuring the conductivity of the solution to determine the acid contained in the solution. Ideally, when the equipment used to measure pH is sufficiently accurate, it is preferable to measure the pH of the liquid to characterize the acidity.
When the pH level is very low and there is a risk that the pH measurement does not give sufficiently accurate results, the measurement may preferably be accompanied by a conductivity measurement.
The pH of the liquid separated off from step b) and/or of the liquid stream or streams withdrawn during the pretreatment is preferably from 0.1 to 7, preferably from 0.5 to 4, more preferably from 0.7 to 2.5.
The conductivity of the liquid separated off from step b) and/or the liquid stream or streams withdrawn during the pretreatment can itself be from 5 to 250 mS/cm, more preferably from 15 to 150 mS/cm, when measured at 70 ℃.
The process of the invention comprises controlling the composition of the impregnation liquor used in step a) so that the acidity of at least one liquid stream withdrawn during the process of the invention is kept constant.
In particular, the process according to the invention comprises a step e) -adjusting the composition of the impregnation liquor used in step a) in order to keep the acidity of the liquid separated from step b) and/or the liquid stream withdrawn during the biomass pretreatment constant throughout the process.
For the purposes of this patent application, it is understood that the acid force "remains constant" when the magnitude characterizing it (pH, conductivity, acid determination, etc.) does not typically vary by ± 10% to 20% throughout the run of the process. Thus, in particular, the composition of the impregnation liquor should be adjusted to ensure that the pH of the liquor separated from step b) and/or said liquid stream withdrawn during biomass pretreatment does not vary by more than 20% from its initial value, in particular from its nominal value, preferably by ± 10% from its initial value (thus, in particular within ± 20%, preferably within ± 10% of the target acidity value). For very low pH values, typically below 1.5, the stability of the pH is considered as a change of ± 0.1 pH units from the nominal value. According to a particular embodiment, when the acidity force is characterized by conductivity, the composition of the impregnation liquor should be adjusted to ensure that the conductivity of the liquid separated from step b) and/or the liquid stream withdrawn during the biomass pretreatment does not vary by more than 20% from its initial value, preferably by not more than 10% from its initial value.
Thus, the acidity of the impregnation liquor introduced into step a) increases (by lowering the pH) when the acidity of the stream considered during the operation of the process of the invention decreases, and conversely, the acidity of the impregnation liquor introduced into step a) decreases (by dilution) when the acidity of the stream considered during the operation of the process of the invention increases.
In particular, the conditioning is performed by adding (or supplying) water and/or acid to the impregnation liquid used in step a).
The addition of water or acid can be added directly to the biomass impregnation step a) or during the preparation of the impregnation liquor. It can be carried out directly on-line or in a plant (mixer, tank, etc.).
Step of recycling
According to a particular embodiment, the process of the invention comprises a step of recycling the liquid separated from step b), the liquid stream withdrawn during the biomass pretreatment and/or the liquid stream withdrawn during the subsequent biomass treatment step (for example by enzymatic hydrolysis and/or alcoholic fermentation) to the impregnation step a).
In the case of recycling, the greater the change in acidity power of the recycle stream, the proportionally greater the adjustment of the impregnation liquor composition.
In particular, the applicant has demonstrated that impregnation produces acid-depleted waste liquids (press liquors and drainage liquors) and a liquid stream with residual acidity withdrawn during biomass pretreatment. Without wishing to be bound by theory, these acidity changes may be due to the alkalinity of the biomass, which neutralizes part of the acid introduced into the impregnation liquor of the process of the present invention. Surprisingly, these streams, in particular the waste streams, also have a buffering effect, which is probably due to the extractable material of the biomass. Thus, recycling them significantly changes the properties of the impregnation liquor. By adding water and the acid described in the present patent application, the applicant has thus observed that it is possible to compensate for the variations in the properties of the impregnation liquor associated with the recycling, so as to maintain constant satisfactory properties in terms of cellulase reactivity of the treated biomass.
Thus, when carrying out the recycling of one or more liquid streams of the process, their composition is analyzed in the same way as the composition of the liquid separated from step b) or of the liquid stream withdrawn during the biomass pretreatment, and the composition of the impregnation liquor used in step a) is adjusted to keep the acidity of said recycled liquid stream constant throughout the process.
In the context of the process of the invention, a liquid having the desired pH is thus prepared to maintain good impregnation throughout the process. A portion of the added acid makes it possible to counteract the alkalinity of the biomass, which can be measured beforehand. This second portion of the addition makes it possible to counteract the buffer properties of the waste liquid. The addition of water makes it possible to adjust the flow rate of the impregnation liquid introduced into step a).
In some cases, one or two washes (purges) may also be arranged immediately after the liquid separation carried out in step b) (pressing or draining) to prevent excessive concentration of molecules obtained from the biomass.
It is also possible to envisage a step of treating the liquid to be recycled in order to purify it and reduce the use of washing.
Similarly, in some cases, for addition, various water sources derived from the process of incorporating the impregnation/pretreatment line may be used. For example, the addition of water may come from the treatment of water, from the treatment of whole stillage obtained from the first distillation column or from the mucilage derived from certain fractions of the main distillation, or a combination of streams of this type. The stillage and the mucilage may optionally be treated to be purified.
Treatment of pretreated biomass by enzymatic hydrolysis and alcohol fermentation
The process according to the invention may in particular comprise, after the pretreatment step c), a step of treating at least part of the pretreated biomass by enzymatic hydrolysis to produce the sugar liquor. According to a preferred embodiment, at least a portion of the sugar liquor is subjected to alcoholic fermentation.
The conditions of enzymatic hydrolysis and continuous or simultaneous fermentation are adapted to the desired product and are known to the person skilled in the art.
The process of the present invention finds particularly advantageous application in processes for the production of sugars from lignocellulosic biomass and in processes for the production of ethanol from said sugar liquors. Such a method is known. A process for the production of sugars from lignocellulosic biomass, comprising a pre-treatment, advantageously steam explosion, followed by enzymatic hydrolysis. The process for producing ethanol from sugars further comprises alcoholic fermentation of the sugars.
In the context of the process of the present invention, the flow rates of the impregnation liquid, water and separated liquid (press liquid or drainage liquid) are measured with any equipment known to the person skilled in the art (e.g. flow meters, volume levels, etc.).
Figures 1 to 4 of the present patent application show, in a non-limiting manner, the implementation of the method according to the invention.
The milled biomass is introduced into the
In the embodiment shown in fig. 2, the impregnation solution is prepared in a step prior to impregnation, in a
The obtained impregnated biomass is then transferred to a
According to one embodiment, the characteristics of the separated
The wet biomass obtained during the separation is then pretreated in a
According to a particular embodiment, the characteristics of the
Figures 3 and 4 illustrate that the separated