OA20069A - Processing of lignocellulosic biomass. - Google Patents

Abstract

Lignocellulosic biomass (11) is processed to produce organic chemicals by (a) subjecting the biomass to a first hydrolysis (14) to hydrolyse hemicellulose, to form a liquid component comprising the products of hemicellulose hydrolysis in solution, and a solid component comprising cellulose and lignin; (b) then subjecting the solid component to a second hydrolysis (20), so as to hydrolyse cellulose and vaporise the resulting products of cellulose hydrolysis; and (c) then condensing (22) the resulting vapours to form an aqueous solution (25) containing the products of cellulose hydrolysis. After the first hydrolysis (14) and before the second hydrolysis (20), the process also comprises subjecting the solid component to a washing step (16). In this washing step (16) the solid component is washed with the aqueous solution (25) that contains the products of cellulose hydrolysis. Hence the resultant solution contains the products of both the first and the second hydrolysis steps (14,20).

Description

Processing of Lignocellulosic Biomass

This invention relates to a process for treating lignocellulosic biomass to produce organic Chemicals, particularly but not exclusively to produce sugars.

As expîained in EP 2 483 331B (Nova Pangaea), there are environmental problems that 5 arise from the use of fossil fuels, so that use of biomass as a source for fuel and organic Chemicals would be advantageous. Woody or lignocellulosic biomass is largely composed of hemicellulose, cellulose and lignin. Cellulose is principally comprised of C6 sugars while hemicellulose comprises both C5 and C6 sugars. Lignin is a complex polymer which gives physical strength to the biomass, but which is tightly bound to the other components. 10 Consequently, it is not straightforward to remove the sugars from the remainder of the biomass. EP 2 483 331B teaches a method of fractionating lignoceliulosic biomass by a sequence of steps. Biomass may befed into a hemicellulose hydrolysis reactor to hydrolyse hemicellulose, so a liquid component includes the products of hemicellulose hydrolysis for example in water, and so that the remaining solid component includes cellulose and lignin. 15 The remaining solid component is then fed to a cellulose hydrolysis reactor which may apply steam at a température of between about 400° and SS0°C, so as to hydrolyse cellulose and vaporise the resulting sugars; and then condensing the resulting vapours. The remaining solids may be in the form of a lignin char.

EP 2 483 331B envisages the potential use of a wide range of different types of biomass, 20 including wood, corn, straw, grass and other cellulose wastes; and indicates that the material may be pretreated for example by drying, and by comminution to create chips or flakes, indicating a preferred size offlakes being of thickness between 1 mm and 3 mm. In addition, where appropriate, the material may be pretreated to remove volatile components such as naturel oils. The hemicellulose hydrolysis reactor may treat the material using 25 steam at a température for example between 170° and 250°C and at an elevated pressure for example between 10 bar(a) and 35 bar(a). These conditions are described in EP 2 483 331B as being sufficient to hydrolyse hemicellulose while minimising dégradation of the biomass material. The sugars produced by hemicellulose hydrolysis will dissolve in water, and may be removed from the biomass using additional water and a counter current water 30 flow; use of a screw press to remove liquid is also mentioned. The resulting solid material consists primarily of cellulose and lignin.

The solid material may be subjected to treatment such as drying and a further size réduction, before being subjected to a process to bring about cellulose hydrolysis. This may be achieved using flash thermolysis using superheated steam, which may for example be at a température between 350° and 550°C, and for example at a pressure between 1 bar(a) and 2 bar(a), such that the bond between lignin and cellulose is broken and the cellulose is hydrolysed into C6 sugars. The vaporised sugars and any other volatile compounds may then be separated from solid matter, and the vapours condensed to form an aqueous 5 solution.

Although EP 2 483 331B describes a range of different ways of performing these steps, research has shown that there are a number of issues that must be resolved if a satisfactory yield of C5 and C6 sugars is to be obtained. For example the hemicellulose hydrolysis tends to produce organic acids such as acetic acid, and also releases alkali components 10 such as potassium ions from the biomass. However the cellulose hydrolysis step will produce a good yield of C6 sugars (or related compounds) only in the absence of significant quantities of alkali; if significant quantifies of alkali or inorganic acid are présent then the cellulose hydrolysis tends to produce smaller molécules such as C1 to C3 aldéhydes and ketones, and gases such as carbon monoxide and carbon dioxide. It is therefore necessary 15 to wash or rinse the solid material output from the hemicellulose hydrolysis step, to remove the alkali materials as well as most of the inorganic acid. This washing or rinsing step has the further benefit of removing any remaining soluble hydrolysis products such as CS or C6 sugars, which would otherwise be destroyed in the subséquent thermolysis step.

It will be appreciated that the Chemical processes that take place when performing the 20 operation referred to as cellulose hydrolysis may be more accurately referred to as thermolysis, pyrolysis, depolymerisatïon or dégradation; the overall resuit is that cellulose is separated from lignin and is broken down into smaller compounds. In this document the process of treating the material with high température steam to create smaller compounds from the cellulose is referred to as cellulose hydrolysis, which is in conformity with the 25 terminology used in EP 2 483 331.

According to the présent invention there is provided a process for treating lignocellulosic biomass to produce organic Chemicals, the process comprising:

(a) subjecting the biomass to a first hydrolysis to hydrolyse hemicellulose, to form a liquid component comprising the products of hemicellulose hydrolysis in solution, and a solid 30 component comprising cellulose and lignin;

(b) then subjecting the solid component to a second hydrolysis, so as to hydrolyse cellulose and vaporise the resulting products of cellulose hydrolysis; and (c) then condensing the resulting vapours to form an aqueous solution containing the products of cellulose hydrolysis;

wherein, after the first hydrolysis and before the second hydrolysis, the process also comprises subjecting the solid component to a washing step, wherein the solid component is washed with the aqueous solution that contains the products of cellulose hydrolysis.

The first hydrolysis would typically be performed at a significantly lower température than the second hydrolysis. For example the first hydrolysis may be at a température no higher 5 than 250°C, whereas the second hydrolysis may be at a température above 350°C.

Furthermore the pressure may be different for these two processes, as may the résidence times.

In one embodiment, acid such as sulphuric acid is added to the biomass before it is subjected to the first hydroiysis. it has been found that the hemicelluiose hydrolysis step is 10 more effective if an acid is présent, and can be carried out at a somewhat lower température, for example no higher than 180°C. To some extent the hemicelluiose hydrolysis reaction may be autocatalytic, because of formation of organic acids such as acetic acid. Nevertheless, the addition of an acid prior to starting the first hydrolysis is bénéficiai in ensuring satisfactory hydrolysis at a lower température than would otherwise 15 be required.

After the washing step, and before the second hydrolysis step, the solid component may be dried. This drying step will evaporate excess moisture.

It will be appreciated that the washing step removes water-soluble inorganic and organic acid and aîkaïi materiai from the solid component, and also removes the products of 20 hemicelluiose hydrolysis that are in solution. It therefore produces washed solid component which can then be subjected to the second hydrolysis to form C6 sugars (rather than Cl to C3 aldéhydes and ketones, and permanent gases). The liquid mixture formed as a resuit of the washing step contains the soluble products of hemicelluiose hydrolysis, which are predominantly C5 sugars (such as xylose), with some C6 sugars (such as glucose and 25 mannose), along with the products of the second hydrolysis, which are predominantly C6 sugars. Consequently, the liquid mixture has a significantly higher total sugar content than would be achieved if the washing step had just used clean water.

After washing with the solution that contains the products of cellulose hydrolysis, the solid component may be subjected to a second washing step using clean water to remove 30 residuaï sugars. This second washing step minimises the sugar that remains in the solid component and is then subjected to the second hydrolysis, which is bénéficiai as the sugar would predominantly be broken down as a resuit of the second hydrolysis. The volume of water used in this second washing step is much less than the volume of the aqueous solution that contains the products of cellulose hydrolysis and that was used for the initial washing step, so that the final concentration of sugars is not significantly reduced by this second washing step.

The products of cellulose hydrolysis are referred to above as C6 sugars, but in practice consist of a mixture which may for example contain glucose, levoglucosan, 5 levoglucosenone, oligomeric anhydrosugars, sugar oligomers and sugars chemically bound to phénol dérivatives. The proportions may dépend on the exact Chemical composition of the solid component that is being treated, and the type of acid présent. The cellulose hydrolysis (or thermolysis) principally produces the volatile compound anhydroglucose, which may be referred to as levoglucosan. If the intention is to produce a 10 sugar solution that can be fermented, it may be bénéficiai to treat this C6 sugar mixture with aqueous acid, which will hâve the effect for example of converting levoglucosan to glucose. In the présent invention the products of cellulose hydrolysis, in solution, are used to wash out the inorganic acid and the alkali materials in addition to the soluble products of hemicelluiose hydrolysis, and the résultant sugar solution is somewhat acidic. Thus the 15 process enables the inorganic acid used in the hemicelluiose hydrolysis to then be used to enhance the conversion of levoglucosan to glucose after the washing step. Hence the acid is effectively used twice, which may make it possible to reduce the total amount of inorganic acid required for the overall process,

The invention will now be further and more particularly described, by way of example only, 20 and with reference to the accompanying drawings in which:

Figure 1 shows a flow diagram for the process of the invention;

Figure 2 shows three modifications to the flow diagram of figure 1 ;

Figure 3 shows an alternative modification to the flow diagram of figure 1 ; and

Figure 4 shows a modification to the flow diagram of figure 2.

Referring to figure 1, the présent invention provides a process 10 for treating biomass 11 such as wood chips so as to obtain CS and C6 sugars by breaking down the hemicelluiose and cellulose polymers within the biomass. The process uses two different hydrolysis steps that are performed at different températures, and may also be carried out at different pressures. However, prior to performing the hydrolysis steps the biomass may be chopped 30 into small preces, and may be heated to evaporate vapours for example of naturallyoccurring oils such as turpentine or eucalyptus oil if these are présent in significant concentration,

After performing any such pre-treatment, the biomass is impregnated 12 with a strong acid, for example with dilute sulphuric acid (i.e. about 1 mole/L) typically at a rate of between 1 - 2 wt % of the dry biomass, before being introduced by a screw conveyor into a reactor 14 in which the biomass is contacted with steam/water at a température of between 150° and 180°C and a pressure of between 6 bar and 10 bar, for example at 165°C and a pressure 5 of 6.5 bar (gauge); there is little air présent. This may be a tube reactor along which the biomass travels along with the high-pressure steam/water. Under these reaction conditions the hemicellulose breaks down mainly to form C5 sugars, with also some C6 sugars, and organic acids, depending on the inhérent composition of the biomass being processed.

At the operating pressure of 6.5 bar, the water at 165°C is liquid as long as the pressure is 10 maintained. As the material leaves the reactor 14 it may be cooled by allowing it to dépressurisé, so that a proportion of the water evaporates, typically about 10%, cooling the remaining biomass to below 100° C. For example the mixture of biomass and hot water may be released in slugs from the reactor. As mentioned above, it is necessary to remove the liquid phase from the treated biomass before it can be subjected to the second 15 hydrolysis step, both to remove sugars and to remove alkali material and any inorganic acid. Although some of the liquid may be removed by compression, this doesn't enable ail the liquid to be expelled. It is therefore préférable to remove the liquid phase by a washing step.

The solid material that has been subjected to the hydrolysis step in the reactor 14 is 20 therefore then washed at step 16, which is described in more detail below.

The washed material is then dried at step 18 to evaporate excess moisture, and may be further comminuted (not shown) to ensure ail the particles small enough to heat up quickly. The material is then introduced, for example with a screw conveyor, into a reactor 20 in which the solid material is contacted with superneated steam at a significantly higher 25 température, for example 550°C. The particles of solid material cool the superheated steam while themselves being heated up. By way of example the material may be fed into a flow of superheated steam at for example 550°C, flowing along a tube substantially in the absence of air, so that the particulate material is carried along with the superheated steam and so effectively subjected to a température in the range for example 380° to 410° for a 30 short period which may for example be between 0.5 seconds and 5 seconds. Under these reaction conditions the cellulose undergoes dégradation or hydrolysis, mainly producing C6 sugar dérivatives which are volatile under these conditions. At the end of the tube the particulate material, which at this stage is a solid iignin char 24, may be separated from the vapours and gases by passing through a cyclone 21, and the vapours then condensed by 35 passage through a heat exchanger 22 (or through a sériés of heat exchangers 22).

The condensed vapours create an output stream 25 which is an aqueous solution of the products of dégradation or hydrolysis of the cellulose, which will primarily consist of C6 sugars, typically in an anhydrous form. For exarnple the products of hydrolysis may be anhydroglucose (which is also called levoglucosan), but there may also be phenolic5 substituted glucose, and phenolic-substituted anhydrosugars as well as oligomeric anhydrosugars and sugar oligomers.

in accordance with the présent invention this output stream 25 of condensed vapours from the cellulose hydrolysis reactor20 is fed back, and used for the washing step 16. Thus the products of the hemicellulose hydrolysis, alkali, and any résultant organic acids, and at 10 least the bulk of the added inorganic acid, are washed out of the solid material in this washing step 16. The resulting aqueous solution 26 therefore contains the C5 sugars produced during hemicellulose hydrolysis, and also the C6 sugars produced during cellulose hydrolysis, and at least the latter may be in an anhydrous form. The aqueous solution also contains the bulk of the acid added at step 12 before the biomass was treated 15 in the hemicellulose hydrolysis reactor 14.

This somewhat acidic aqueous solution 26 containing C5 and C6 sugars may be the final product of the process 10.

Referring nowto figure 2, this shows three modifications to the process 10 of figure 1, and any one or more of these modifications may be used. The process 30 of Figure 2 illustrâtes 20 the use of ail three modifications; in ali other respects the processes 10 and 30 are the same, and the same reference numbers are used.

In one modification, the somewhat acidic solution 26 is then heated, at step 32, typically to about 120°C for 30 minutes, to ensure that the anhydrous sugars are hydrolysed. This hydrolysis of the anhydrous sugars is cataiysed by the presence of the inorganic acid. 25 Additional acid may be added to the somewhat acidic solution 26 if required. The anhydroglucose (predominantly, levoglucosan) and any phenolic-substituted glucose, oligomeric anhydrosugars and sugar oligomers are thereby converted to glucose.

in a second modification, the remaining acid may be neutraiised by adding, at step 34, a base, for example slaked lime (calcium hydroxide), to obtain a substantially neutral pH, i.e.

³⁰ pH 7, so that the overall process produces a neutral aqueous sugar solution 36 which contains both C5 (hemicellulosic) and C6 sugars, and is not acidic. This step 34 may be carried out after performing the hydrolysis step 32, or if there is no requirement to hydrolyse the anhydrous sugars, then the step 34 of adding the base may be applied to the somewhat acidic solution 26, without performing the hydrolysis step 32.

It will be appreciated that after the solid material has been washed, at step 16, using the aqueous C6 sugar solution, that is to say the output stream 25, some of that 06 sugar solution will remain within or in contact with the solid material. Such remaining sugar is likely to be destroyed during the high température cellulose hydrolysis step 20. Hence, in 5 a third modification, after washing the solid material using the aqueous 06 sugar solution 25, it may be advantageous to subject the solid material to a further wash or rinse with clean water (indicated by reference 38), to wash out the residual 06 sugars. This may be demineralised water. The sugar solution obtained through this further washing or rinsing step 38 is combined with the somewhat acid solution 26. The volume of clean water used 10 for this further washing or rinsing step 38 should be significantly less than the volume of the aqueous 06 sugar solution, that is to say the output stream 25, used for the initial washing step 16, so the concentration of sugar in the somewhat acidic aqueous solution 26 is not significantly reduced by the addition of the clean water.

It will be appreciated that the process 10 or 30 of the présent invention combines the 05 15 sugar solution produced by the hemicellulose hydrolysis 14 with the 06 sugar solution produced by the cellulose hydrolysis 20. This has the advantage that the anhydrous 06 sugars produced în the cellulose hydrolysis step 20 can readily be hydrolysed to the hydrous 06 sugars, because most or ail of the acid that would conventionally be required to catalyse this hydrolysis is already présent in the 05 sugar solution. Thus the inorganic 20 acid which is added at 12 to the biomass to enhance the first hydrolysis step 14 is subsequently made use of to perform the subséquent hydrolysis step 32. The acid is thereby made use of twice, so less acid is required in total, and less basic material is required to neutralise the acid.

Referrïng now to figure 3, this shows an alternative process 40 which is a modification to 25 the process 10 of figure 1, in which the same reference numerals are used to refer to the same features. The process 40 differs from the process 10 in that no inorganic acid is added to the biomass 11 before performing the first hydrolysis step in the hydrolysis reactor 14. It may therefore be necessary to operate the hydrolysis reactor 14 at a higher température and pressure than described above in relation to the process 10. The washing 30 step 16, the drying step 18 and the operation of the cellulose hydrolysis reactor 20 are performed in the same way as described above, One conséquence of operating in this way is that the aqueous solution 26a produced from the washing step 16 contains the C5 and C6 sugars produced by the hydrolysis of hemicellulose and also the anhydro C6 sugars produced by the hydrolysis of cellulose, as described above, but that the aqueous solution 35 26a is not acidic. This aqueous solution 26a may be the output product of the process 40.

if it is necessary to hydrolyse the products of the cellulose hydrolysis reactor 20 to form sugars, this may be achieved by adding an inorganic acid to the solution 26a, and then performing hydrolysis by a heating step 32, and optionally also a neutralisation step 34, as described above in relation to figure 2. Furthermore, the process 40 may also be modified 5 to incorporate the additional wash or rinse with clean water 38 as described above in relation to figure 2.

Referring now to figure 4, this shows a process 50 which is a modification to the process 30 of figure 2, in which the same reference numerals are used to refer to the same features. The process 50 differs from the process 30 in that an inorganic acid 12 is added to the 10 output stream 25 that is the aqueous solution of the products of dégradation or hydrolysis of the cellulose, output from the reactor 20, and the resulting acidified solution is heated at step 32, typically to about 120°C for 30 minutes, to ensure that the anhydrous sugars are hydrolysed. Then, as in the processes 10, 30 and 40, the solution is used in the washing step 16. Consequently, the liquid outflow from the washing step 16 is a somewhat acidic 15 solution 26b which contains both C5 sugars and C6 sugars which are already in their hydrolysed form. This aqueous solution 26b may be the output product of the process 50.

If a neutral solution of C5 and C6 sugars is required, this may be achieved by adding, at step 34, a base, for example slaked lime (calcium hydroxide), to obtain a substantially neutral pH, i.e. pH 7, so that the overall process 50 produces a neutral aqueous sugar 20 solution 36 which contains both C5 and C6 sugars.

In a modification to the process 50, the solution output from the hydroiysing heating step 32 may be subjected to a neutralisation step équivalent to step 34 before being used to perform the washing step 16. This modification is not shown.

A further benefit that the invention provides is that the output stream 25 of condensed 25 vapours from the cellulose hydrolysis reactor 20 may contain phenolic compounds, in addition to the C6 sugars. As a general rule these phenolic compounds are not required or useful in the résultant sugar solution 26. The washing step 60 brings the output stream 25 into intimate contact with the solid material, and it is surmised that much of these phenolic compounds will be absorbed onto the solid material, rather than being carried through into 30 the résultant sugar solution 26,

The following Examples show the effect of the washing step 16 on the performance of the process.

Example 1

Birch wood that had been subjected to the first hydrolysis step 14, and so containing the monomerized hemi-cellulosic sugars as well as the sulphuric acid used to catalyze the hemicehuiose hydrolysis, was washed either three times with the aqueous output stream 25 of condensed vapours from the cellulose hydrolysis reactor 20, and subsequently once 5 with pure demineralised water or four times with pure demineralised water. A mass ratio of approximately 1:2 (wet pretreated material : liquid stream 25) was used in each washing step. The washed material was isolated by nitration as part of each washing step.

The two washed materials were dried and subjected to the cellulose hydrolysis step 20 at 400°C in the presence of superheated steam as described above.

As shown in Table 1 a total sugar yield of 32.1 % was obtained from the cellulose hydrolysis step 20 (pyrolysis) of the material washed four times with pure demineralized water. Surprisingly the yield obtained from the cellulose hydrolysis step 20 (pyrolysis) of material washed three times with the aqueous output stream 25 and then once with water was practicaily identical at 31.1%.

Table 1. Total sugar yield from pyrolysis of pretreated material washed with demineralized water, or with the aqueous stream 25 and demineralised water.

	Total sugars yield from pretreated material in pyrolysis (%)
Pretreated material washed 4 times with pure water	32.1
Pretreated material washed 3 times with aqueous stream 25 (pyrolysis condensate) and once with pure water	31.1

Example 2

Birch wood that had been subjected to the first hydrolysis step 14, and so containing the 20 monomerized hemi-cellulosic sugar as well as the sulphuric acid used to catalyze the hemicellulose hydrolysis, was washed three times with fresh pyrolysis condensate (i.e. the aqueous stream 25) and subsequently two times with pure demineralized water. Solid-liquid séparation after each wash was done by vacuum filtration. The second hydrolysis step 20 (pyrolysis) of the washed material was carried out on samples taken 25 after each washing step, to examine the feasibility of using the aqueous output stream 25 (pyrolysis condensate) as washing medium instead of using solely pure demineralized water. A mass ratio of 1:2 (wet pretreated material : pyrolysis condensate) was used in each washing step.

The pyrolysis condensate (i.e. the aqueous stream 25) contains no sulphuric acid and hence the sulphuric acid concentration in the filtrate liquid 26 is a good indicator of residual 5 sulphuric content in the washed solid material. The sulphuric acid content in the filtrate liquid after each successive washing step is shown in Table 2 below. It can be seen that the sulphuric acid wt.% decreases as a function of consecutive washes and over three washing steps with fresh pyrolysis condensate the sulphuric acid content drops from 0.21 wt.%, to 0.08 wt.%, and then to 0.05 wt.%, A subséquent wash with pure water brings the 10 sulphuric acid concentration of the filtrate below 0.01 wt.%.

Table 2. Sulphuric acid content in filtrate liquid as a function of washing.

Filtrate No.	Sulphuric acid content in filtrate (wt.%)
Pyrolysis condensate washes
1st	0.21
2nd	0.08
3rd	0.05
Water washes
4th	<0.01
5th	<0.01

Table 3 shows the yield of levoglucosan obtained from the second hydrolysis step 20 (pyrolysis) of the solid material washed either 3 times with condensate, 3 times with 15 condensate and once with pure demineralised water or 3 times with condensate and twice with pure demineralised water. respectively. The yield is given in relative carbon% of ail the gaseous products formed.

Table 3. Pyrolysis yields of levoglucosan as a function of washing

Solid product after washing	Levoglucosan yield (relative yield în % from GC analysis)
3rd washing (3 x pyrolysis condensate)	39.0
4Ih washing (3 x pyrolysis condensate + 1 x pure	39.9

water)
5th washing (3 x pyrolysis condensate + 2 x pure water)	21.1

The second hydrolysis step 20 (pyrolysis) if carried out on material which contains significant amounts of suiphuric acid, such as unwashed material or material washed only once with either water or pyrolysis condensate, will lead to low yields of levoglucosan (<20%). Surprisingîy, it can be seen from Table 3 that the yield of levoglucosan after 5 washing three times solely with the aqueous stream 25 (i.e. pyrolysis condensate) , which is 39.0%, is practically identical with the levoglucosan yield obtained after washing three times with the aqueous stream 25 (pyrolysis condensate) and subsequently once with pure demineralised water (39.9%). The yield did not increase further if the material was washed further with pure water and indeed the yield actually dropped to 21.1% if the material was 10 given a second wash with demineralised water. This suggests that the material can be washed too much; this may be becausè ïow residual levels of suiphuric acid are bénéficiai to the formation of levoglucosan in the second hydrolysis step 20.

Claims

Claims (8)

1. Claims

   1. A process for treating lignocellulosic biomass to produce organic Chemicals, the process comprising:

   (a) subjecting the biomass to a first hydrolysis at a température no higher than 250°C to hydrolyse hemicellulose, to form a liquid component comprising the products of hemicellulose hydrolysis in solution, and a solid component comprising cellulose and lignin;

   (b) then subjecting the solid component to a second hydrolysis at a température above 350°C, so as to hydrolyse cellulose and vaporise the resulting products of cellulose hydrolysis; and (c) then condensing the resulting vapours to form an aqueous solution containing the products of cellulose hydrolysis wherein, after the first hydrolysis and before the second hydrolysis, the process also comprises separating the liquid and solid components and subjecting the solid component to a washing step, wherein the solid component is washed with the aqueous solution that contains the products of cellulose hydrolysis, to produce a résultant aqueous sugar solution.
2. 2. A process as claimed in claim 1 wherein, after the washing step and before the second hydrolysis, the process also comprises subjecting the solid component to a drying step.
3. 3. A process as claimed in either one of claims 1 or 2 wherein a strong acid, such as suiphuric acid, is added to the biomass before it is subjected to the first hydrolysis.
4. 4. A process as claimed in any one of the previous claims wherein, after washing with the solution that contains the products of cellulose hydrolysis, the solid component is then subjected to a second washing step using clean water to remove residual sugars.
5. 5. A process as claimed in daim 4 wherein the volume of water used in this second washing step is less than the volume of the aqueous solution that contains the products of cellulose hydrolysis and that was used for the initial washing step.
6. 6. A process as claimed in any one of the previous claims, wherein a basic material is added to the résultant aqueous sugar solution, to neutralise remaining acid.
7. 7. A process as claimed in any one of claims 1 to 5, wherein the aqueous solution containing the products of cellulose hydrolysis is hydrolysed to glucose before being used in the washing step.
8. 8. A process as claimed in claim 7, wherein the aqueous solution containing the products of cellulose hydrolysis, after being hydrolysed to glucose, is then neutralized before being used in the washing step.