A METHOD FOR PROCESSING BIOMASS DIGESTATE

Abstract

A method for processing biomass digestate is disclosed. The method comprises the steps of—providing a biomass digestate (BD), —subjecting the biomass digestate to a separation step (SEP) into a liquid fraction (LF) and a solid biomass digestate fraction (SBD), —subjecting the solid biomass digestate fraction (SBD) to an acidic wash step (AW) at a pressure below 200 kPa (2 bar) to obtain a washed biomass digestate (WBD), —separating (SEP) the washed biomass digestate (WBD) into a liquid wash fraction (LW) and a solid wash fraction (SW), —posttreating (POST) the solid wash fraction (SW) to obtain a posttreated solid wash fraction (PSW) and—anaerobic digesting (AD) the posttreated solid wash fraction (PSW) to obtain a posttreated biomass digestate (PBD) wherein the amount of phosphorus in the solid wash fraction (SW) is reduced compared to amount of phosphorus in the solid biomass digestate fraction (SBD).

Claims

1. A method for processing biomass digestate, the method comprising the steps of: providing a biomass digestate, subjecting the biomass digestate to a separation step into a liquid fraction and a solid biomass digestate fraction, subjecting the solid biomass digestate fraction to an acidic wash step at a pressure below 200 kPa (2 bar) to obtain a washed biomass digestate, separating the washed biomass digestate into a liquid wash fraction and a solid wash fraction, posttreating the solid wash fraction to obtain a posttreated solid wash fraction and anaerobic digesting the posttreated solid wash fraction to obtain a posttreated biomass digestate, wherein the amount of phosphorus in the solid wash fraction is reduced compared to amount of phosphorus in the solid biomass digestate fraction.

2. The method according to claim 1, wherein the acidic wash step is non-pressurized.

3. The method according to claim 1, wherein the amount of phosphorus in the solid wash fraction is less than 10% by weight of the phosphorus in the biomass digestate.

4. (canceled)

5. The method according to claim 1, wherein the pH in the acidic wash step is between 0 and 7.

6. The method according to any claim 1, wherein the temperature in the acidic wash step is between 50 to 100 degrees Celsius.

7. (canceled)

8. (canceled)

9. (canceled)

10. (canceled)

11. The method according to claim 1, wherein the acid in the acidic wash step is an organic acid.

12. The method according to any of the preceding claims, wherein the amount of phosphorus in the liquid wash fraction is reduced to obtain a low phosphorus liquid fraction.

13. (canceled)

14. (canceled)

15. (canceled)

16. The method according to claim 1, wherein the liquid wash fraction is recirculated into the acidic wash step.

17. The method according to claim 1, wherein the biomass digestate is provided by heating a soft biomass in a pretreatment step followed by anaerobic digesting of the soft biomass to obtain the biomass digestate.

18. (canceled)

19. (canceled)

20. The method according to claim 1, wherein the posttreatment temperature is between 40 and 230 degrees Celsius.

21. The method according to claim 1, wherein the posttreatment is performed by base treatment.

22. The method according to claim 1, wherein the posttreatment step is performed at a pressure between 1 MPa (10 bar) and 2 MPa (20 bar).

23. (canceled)

24. (canceled)

25. The method according to claim 1, wherein the posttreatment is performed by steam explosion and/or laccase treatment.

26. The method according to claim 1, wherein the posttreatment is performed by bacteria or fungi treatment.

27. The method according to claim 1, wherein furfural and 5-HMF and 2-furoic acid are generated in a combined amount of less than 5% w/w relative to total dry matter in the post treatment step.

28. (canceled)

29. The method according to claim 1, wherein the method further comprises a further separation step after anaerobic digesting the posttreated solid wash fraction to obtain a liquid posttreated biomass digestate fraction and a solid posttreated biomass digestate fraction.

30. The method according to claim 29, wherein the method further comprises a drying step of the solid posttreated biomass digestate fraction to obtain a dried posttreated biomass digestate.

31. The method according to claim 30, wherein the amount of nitrogen in the dried posttreated biomass digestate is reduced by at least 50% by weight of the nitrogen comprised in the biomass digestate entering the process.

32. (canceled)

33. (canceled)

34. The method according to claim 1, wherein biogas is obtained from at least the anaerobic digesting step of the posttreated solid wash fraction.

35. The method according to claim 1, wherein the method further comprises recirculation of at least a part of a liquid fraction from any separation step to any anaerobic digesting step and/or the pretreatment step.

Description

FIGURES

[0120] FIG. 1 illustrates a method for processing biomass digestate according to an embodiment of the invention.

[0121] FIG. 2 illustrates a method for processing biomass according to an embodiment of the invention.

[0122] FIG. 3 illustrates removal of phosphorus from a solid biomass digestate fraction within 1 hour as a result of pH in the acidic wash step.

[0123] FIG. 4 illustrates removal of phosphorus from a solid biomass digestate fraction as a result of pH, temperature and time.

[0124] FIG. 5 illustrates removal of phosphorus from liquid wash fractions.

[0125] FIG. 6 illustrates the amount of additional methane produced as a result of different post-treatments or no posttreatment.

[0126] FIG. 7 illustrates the amount of additional methane produced as a result of different post-treatments relative to no post-treatment.

[0127] FIG. 8 illustrates removal of phosphorus from a solid biomass digestate fraction after incubation at 50° C. during 24 h at various starting pH values.

[0128] FIG. 9 illustrates removal of phosphorus from a solid biomass digestate fraction as a function of time at four different starting pH values at 50° C.

[0129] FIG. 10 illustrates removal of phosphorus from a solid biomass digestate fraction after 24 h at different starting pH values at 50° C. and 80° C.

DETAILED DESCRIPTION

[0130] As used herein, the term “non-pressurized” is intended to mean ambient pressure, which at average sea level is a pressure around 1 bar=101 kPa.

[0131] As used herein, the term “pressurized” is intended to mean a pressure significantly higher than ambient pressure. Usually this may be around 1-2 MPa (10-20 bar), especially in the field of biogas production.

[0132] As used herein “biomass digestate” is intended to mean a product of anaerobic digestion AD of soft biomass and represents the digested material, which is removed from the AD reactor (digestor) after recovery of biogas. Digestate is normally liquid.

[0133] As used herein, the term “soft biomass” is intended to mean non-wood lignocellulosic biomass, comprising cellulose, hemicellulose and lignin. Soft biomass may e.g. be wheat straw, corn stover, rice straw, grass, and bagasse.

[0134] In an embodiment of the invention, the term “soft biomass” is intended to mean cellulosic and herbaceous types of biomass, such as wheat straw, corn stover, rice straw, grass, and bagasse.

[0135] As used herein, the term “dry matter” is intended to mean the residual when water is evaporated.

[0136] Lignocellulosic biomass usually comprises crystalline cellulose fibrils intercalated within a loosely organized matrix of hemicellulose and sealed within an environment rich in hydrophobic lignin. While cellulose itself comprises long, straight chain polymers of D-glucose, hemicellulose is a heterogeneous mixture of short, branched-chain carbohydrates including monomers of all the 5-carbon aldopentoses (C5 sugars) as well as some 6-carbon (C6) sugars including glucose and mannose. Lignin is a highly heterogeneous polymer, lacking any particular primary structure, and comprising hydrophobic phenylpropanoid monomers. Suitable lignocellulosic biomass typically comprises cellulose in amounts between 20 and 50% of dry mass prior to pretreatment, lignin in amounts between 10 and 40% of dry mass prior to pretreatment, and hemicellulose in amounts between 15 and 40%.

[0137] As used herein, the term “liquid fraction” is intended to mean the fraction having the lowest dry matter after a separation step. The amount of suspended solids is normally around 4% per weight, but typically varies from 0 to less than 10%.

[0138] As used herein, the term “solid fraction” intended to mean the fraction having the highest dry matter after a separation step. The amount of suspended solids is normally around 20-25% per weight, but may vary from 10-95%.

[0139] As used herein, the term “anaerobic digestion” is intended to mean a collection of processes by which microorganisms break down break down biodegradable material in the absence of oxygen. Anaerobic digestion usually begins with bacterial hydrolysis of the input materials. Insoluble organic polymers, such as carbohydrates, are broken down to soluble derivatives that become available for other bacteria. Acidogenic bacteria may then convert the sugars and amino acids into carbon dioxide, hydrogen, ammonia and organic acids. These bacteria may convert these resulting organic acids into acetic acid, along with additional ammonia, hydrogen, and carbon dioxide. Finally, methanogens may convert these products to methane and carbon dioxide. Anaerobic digestion is widely used as a source of renewable energy. The process produces a biogas, comprising mostly methane and carbon dioxide.

[0140] As used herein, the term “pretreatment” is intended to mean a treatment of a biomass prior to a first anaerobic digestion step.

[0141] As used herein, the term “posttreatment” is intended to mean a treatment of a biomass digestate subsequent to the acidic wash step and prior to anaerobic digestion of the posttreated solid wash fraction. The posttreatment increases the yield of biogas in the subsequent anaerobic digestion (of the posttreated solid wash fraction). A purpose of the posttreatment is thus to increase the digestability of the solid wash fraction prior to anaerobic digestion. Thus, the posttreatment step could be considered a digestion preparation step, a biomass preparation step or simply a preparation step. Alternatively, the posttreatment step could be considered treatment for maturing the biomass for digestion i.e. a biomass maturation step.

[0142] The aim of posttreatment step is to loosen, degrade or dissolve the lignin layer that protects the cellulose and hemicellulose and/or reduce the crystallinity of cellulose in order to make the biomass more accessible for digestion.

[0143] The posttreatment step includes very diverse processes such as biological-, non-biological, chemical and physiochemical processes. Hence, post-treatment step may be a steam explosion, laccase treatment, base treatment, dilute acid treatment, thermal treatment, dissolution in ionic liquids and subsequent precipitation, dissolution in molten salt hydrates, or the organosolv process, or combinations such as steam explosion and laccase.

[0144] As used herein nitrogen (N) as is intended to mean the sum of organic bound nitrogen, such as the nitrogen in amines, and inorganic bound nitrogen, such as e.g. NH.sub.3 and NH.sub.4.sup.+.

[0145] As used herein phosphorus (P) is intended to mean the sum of organic bound P and inorganic bound P, such as e.g. PO.sub.4 ions (e.g. PO.sub.4).

[0146] As used herein “nutrients” is intended to mean macronutrients for plants, such as nitrogen (N), phosphorus (P), potassium (K), calcium (Ca) and sulfur (S).

[0147] As used herein “strong acid” is meant to be an acid having a pKa below 3.

[0148] As used herein “weak acid” is meant to be an acid having a pKa above 3.

[0149] As used herein, the singular forms “a”, “an” and “the” include plural referents unless the context clearly dictates otherwise.

[0150] As used herein, “at least one” is intended to mean one or more, i.e. 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, etc.

[0151] As used herein, the term “biogas” is intended to mean methane gas and carbondioxide gas obtained from degradation of biological material, such as biomass.

[0152] As used herein, the term “inoculum” is intended to mean organic material containing bacteria, such as digested (degassed) biomass from an existing biogas facility or animal waste.

[0153] As used herein, the term “dry matter” is intended to mean the residual when water is evaporated.

[0154] As used herein, the term volatile solids (VS) shall mean the organic part of dry matter.

[0155] Separation may for example be performed with a screw press, filter press or decanter.

Abbreviations

[0156] VS=volatile solids

[0157] 5-HMF=5-(hydroxymethyl)furfural

[0158] TS=total solids

[0159] Referring to FIG. 1, a method for processing biomass digestate according to an embodiment of the invention is disclosed.

[0160] Biomass digestate (which may be pretreated) is separated into a solid biomass digestate fraction, such as a fiber fraction, and a liquid fraction. The liquid fraction contains a lower phosphorus concentration compared to the digestate and can be used as fertilizer.

[0161] The solid fraction is mixed with acid in a wash reactor in which phosphorus will be dissolved from fibers into the liquid phase. Afterwards the slurry is separated into a solid washed fiber fraction and a liquid wash fraction.

[0162] The solid wash fraction (fiber fraction) is posttreated to increase the digestibility of the fiber. The posttreated solid wash fraction is transferred to another biogas reactor and a second anaerobic digestion process is performed to produce more biogas.

[0163] Referring to FIG. 2, a method for processing biomass digestate according to an embodiment of the invention is disclosed.

[0164] Biomass digestate (which may be pretreated) is separated into a solid biomass digestate fraction, such as a fiber fraction, and a liquid fraction. The liquid fraction contains a lower phosphorus concentration compared to the digestate and can be used as fertilizer. The solid fraction is mixed with acid in a wash reactor in which the phosphorus will be dissolved from fibers into the liquid phase. Afterwards the slurry is separated into a solid washed fiber fraction and a liquid wash fraction. The liquid wash fraction may e.g. be transferred to an ion exchange column, in which the phosphorus binds to the resin in the ion exchange column. The ion exchanged liquid wash fraction contains a very low amount of phosphorus and may advantageously be transferred back to the wash reactor.

[0165] The phosphorus bound to the resin may be released by e.g. increasing the pH with NaOH, and thereby producing Na.sub.3PO.sub.4. The solid wash fraction (fiber fraction) is post treated to increase the digestibility of the fiber. The posttreated solid wash fraction is transferred to another biogas reactor to produce more biogas. After anaerobic digestion in a biogas process, the slurry may be pressed i.e. separated into a posttreated biomass digestate liquid fraction and a posttreated biomass digestate solid fraction, which may be referred to as a lignin fraction, since this fraction comprises high amounts of lignin. The posttreated biomass digestate liquid fraction may be transferred back to the biogas reactor. The lignin fraction can then be dried. In the dryer, the ammonium will evaporate and the lignin will be dry and of a high purity.

EXAMPLES

Example 1: Washing Phosphorus Out of Fiber with Sulphuric Acid and Hydrochloric Acid

[0166] This example describes how to wash the phosphorus out of biomass digestate, such as a solid biomass digestate fraction, with acid. A fixed amount of fiber i.e. solid biomass digestate has been mixed with different types of acid with varying pH.

[0167] Materials and Methods: [0168] Fiber, produced from separating digestate from a biogas plant into a solid biomass digestate fraction [0169] Water [0170] Sulphuric acid (H.sub.2SO.sub.4) [0171] Hydrochloric acid (HCl)

[0172] Four washes were made to test sulphuric acid and hydrochloric acid at different pH. 900 g of water was mixed with sulphuric acid and hydrochloric acid, respectively. Two samples were mixed to a pH of 1 and two samples to a pH of 3. 90 g of fiber was added to each of the four samples and mixed. After 1 h at 25° C., fiber and wash water were separated and phosphorus was measured the liquid wash fraction as well as in an untreated fiber sample, in order to find out how much phosphorus was separated into the liquid wash fraction.

[0173] Results:

[0174] The results show that pH has a large impact on the dilution of phosphorus into the wash-liquid within the first hour. The lower the pH, the more phosphorus is removed from the fiber, as seen on FIG. 3.

Example 2: Washing Phosphorus Out of the Solid Biomass Digestate Fraction with Oxalic Acid Varying pH, Incubation Temperature and -Time

[0175] This example describes how to wash the phosphorus out of solid biomass digestate fraction with oxalic acid. A fixed amount of solid biomass digestate fraction has been mixed with oxalic acid at varying pH, incubation temperature and incubation time.

[0176] Materials and Methods: [0177] Solid biomass digestate fraction (fiber fraction, produced from separating digestate from a biogas plant) [0178] Water [0179] Oxalic acid (C.sub.2H.sub.2O.sub.4)

[0180] A Design of Experiments (DOE) software “MODDE Go” (version 12.1.0.5491, Mar. 23, 2018) was used to design the experiment and analyze the results. Washes were made with oxalic acid in which three factors were varied; pH of solution, incubation temperature and incubation time. The pH were 0.79, 0.92 and 1.26, the incubation temperatures were 40° C., 70° C. and 100° C., and the incubation times were 10 min, 2 hours, and 3 hours and 50 min. For each wash, 900 g of water was mixed with oxalic acid to the desired pH and 90 g of solid biomass digestate fraction was added and mixed. The factors were combined as shown in Table 1.

TABLE-US-00001 TABLE 1 Scheme of how the factors are combined in the different samples. pH of acid Incubation Sample solution temperature (° C.) Incubation time 1 1.26 40 10 min 2 1.26 100 10 min 3 1.26 70 2 hours 4 1.26 40 3 hours 50 min 5 1.26 100 3 hours 50 min 6 0.79 40 10 min 7 0.79 100 10 min 8 0.79 70 2 hours 9 0.79 40 3 hours 50 min 10 0.79 100 3 hours 50 min 11 0.92 40 10 min 12 0.92 100 10 min 13 0.92 70 2 hours 14 0.92 70 2 hours 15 0.92 70 2 hours 16 0.92 40 3 hours 50 min 17 0.92 100 3 hours 50 min

[0181] After each wash, the washed biomass digestate was separated into a solid fraction and a liquid wash fraction and phosphorus was measured on the liquid wash fraction as well as on an untreated solid biomass digestate fraction sample, in order to find out how much phosphorus was diluted (i.e. removed from the solid fraction) in the liquid wash fraction.

[0182] Results:

[0183] As the experiment was designed with use of a statistical design, a function is calculated on basis of all the data points by the program MODDE Go, and the result of the experiments can thus be seen in FIG. 4. Selected raw data points are shown in table 2a-2b, however one should not rely entirely on a single value but instead look at the function calculated on basis of all the data points as shown in FIG. 4. Sample 13, 14 and 15 are replicates, and from these the uncertainty of the results is found to be +/−1%. The function has a high R2 value of 88% which is the percent of the variation of the response explained by the model.

[0184] The results show that it is possible to remove 99% of the phosphorus from the solid biomass digestate fraction. From FIG. 4, one can see that the lower the pH is and/or the higher the temperature and/or the longer the washing time, the more phosphorus is removed from the solid biomass digestate fraction (and thus present in the liquid wash fraction).

TABLE-US-00002 TABLE 2a Raw data points used to calculate the function illustrated in FIG. 4. Amount of phosphorus removed from the solid biomass digestate fraction by washing with an aqueous acidic solution. Sample 1 2 3 4 5 6 7 8 9 10 P removal 75% 85% 90% 89% 94% 89% 95% 96% 94% 96%

TABLE-US-00003 TABLE 2b Raw data points used to calculate the function illustrated in FIG. 4. Amount of phosphorus removed from the solid biomass digestate fraction by washing with an aqueous acidic solution. Sample 11 12 13 14 15 16 17 P removal 85% 91% 96% 94% 95% 91% 99%

[0185] Another series of experiments were conducted. The treatment was performed at 50° C. for 24 hours. The starting pH was varied from 2 to 8.7. At these conditions the pH changes during the treatment, but the reported values are starting values, i.e. measured pH immediately after mixing of water, oxalic acid and fibers. The procedure was the same as described above.

[0186] Results:

[0187] FIG. 8 shows the percentage of phosphorus removed from the solid biomass digestate fraction after incubation at 50° C. during 24 h at various starting pH values. It is seen that the phosphorus can be removed efficiently up until at least pH 5.75 under these conditions. FIG. 10 shows a comparison of selected experiments from FIG. 8 and corresponding experiments run at 80° C. It can be concluded that the temperature plays a minor role at the conditions investigated. The removal of phosphorus was followed as a function of time for four different starting pH values. The results are plotted in FIG. 9 and show that most of the phosphorus is washed out during the first six hours for the lower pH values of 3.2 and 3.8. Incubation times of up to 48 hours are needed to reach the same level of phosphorus removal for pH values of 4.7 and 5.8.

Example 3: Removing Phosphorus from the Wash-Liquid Fraction

[0188] This example describes how to remove the phosphorus by means of ion exchange from the liquid wash fraction obtained from the acidic wash step.

[0189] An acid wash step has been performed prior. The wash was made by mixing 900 g of water with oxalic acid to a pH of 1 and adding 90 g of fiber (solid biomass digestate fraction produced from separating digestate from a biogas plant) with an incubation temperature of 25° C. and an incubation time of 15 hours. Afterwards the washed biomass digestate was separated into a solid wash fraction (fiber fraction) and liquid wash fraction, and the liquid wash fraction was treated.

[0190] Materials and Methods: [0191] Liquid wash fraction obtained from acid wash of solid biomass digestate fraction (type of wash is described above) [0192] Resin 1 (Lewatit FO 36, Lanxess) [0193] Resin 2 (Amberlite MB 3, Merck)

[0194] 20 g of liquid wash fraction was mixed with 20 g of resin 1, and 20 g of liquid wash fraction was mixed with 20 g of resin 2 in blue cap bottles. The bottles were incubated at 50° C. for an hour with stirring, and afterwards they were centrifuged to separate the resins from the liquid wash fraction. Phosphorus was measured in the liquid wash fraction without subjecting it to ion exchange, and the two ion exchange treated liquid wash fractions to find out how much phosphorus the two resins are able to remove.

[0195] Results:

[0196] By using ion exchange, it is possible to remove 99% of the phosphorus in the liquid wash fraction obtained from acid wash of solid biomass digestate fraction, as seen in FIG. 5. Furthermore, both resins tested can be used for phosphorus removal.

Example 4: Extra Methane as a Result of Post-Treatment

[0197] This example describes how to produce extra biogas from biomass digestate as a result of different types of post-treatment of solid wash fractions.

[0198] Prior to the post-treatments, an acidic wash of solid biomass digestate fractions was performed. The acidic wash was made by mixing 891 g of water with 9 g of oxalic acid so it had a concentration of 0.1 mol/L and adding 90 g of solid biomass digestate (produced from separating digestate from a biogas plant) with an incubation temperature of 50° C. and an incubation time of 3 hours. Afterwards the washed biomass digestate was separated into a solid wash fraction and a liquid wash fraction, and the solid wash fraction was post-treated.

[0199] Materials and Methods: [0200] Solid wash fraction from acid wash (type of wash is described above) [0201] Water [0202] Citric acid [0203] Sodium hydroxide (NaOH) [0204] Laccase [0205] Inoculum (reactor liquid from a biogas plant)

[0206] Five different samples for posttreatment and subsequent anaerobic digestion were prepared. The first sample was just solid wash fraction from acid wash with no posttreatment. The second sample was solid wash fraction from acid wash, which was post-treated with steam explosion. The third sample was solid wash fraction from acid wash, which was post-treated with laccase. The fourth sample was solid wash fraction from acid wash, which was post-treated with steam explosion and afterwards laccase.

[0207] The fifth sample was solid wash fraction from acid wash, which was posttreated with sodium hydroxide. The steam explosion was performed by mixing 40 g of solid wash fraction and 160 g of water in a Parr Reactor, which was run for 15 min at 180° C. The laccase treatment was performed by mixing 8 g of solid wash fraction with 90 g of a 0.1 M citric acid buffer adjusted to pH 5 with NaOH. 0.6 g laccase/g TS solid wash fraction was added and the sample was stirred for 24 hours at 250 rpm in a shaking incubator at 45° C. The base treatment was performed by mixing 15 g of solid wash fraction with 90 g of water and adding NaOH to reach a pH of 12. The sample was heated to 100° C. for 20 hours. After each post-treatment, the five samples were adjusted to a pH of 8 with NaOH/HCl and mixed with inoculum and anaerobic digested for 15 days at a temperature of 52° C.

[0208] Results: Additional biogas was obtained for all samples as depicted in FIGS. 6 and 7. The results depicted in FIG. 6 illustrates the additional methane produced by processing digestate including a posttreatment step or not.

[0209] The results depicted in FIG. 7 are normalized to the result obtained when no post-treatment was performed. Steam explosion resulted in 138% extra methane, laccase treatment resulted in 200% extra methane. Combining the two methods by posttreating the solid wash fraction with steam explosion followed by laccase treatment resulted in a surprising 413% extra methane. Base treatment resulted in 3510% extra methane.

[0210] Base treatment was further explored with experiments run at different temperatures varying from 50 degrees Celsius to 120 degrees Celsius. A satisfying result was obtained for all tested temperatures in between 50 degrees Celsius and 120 degrees Celsius.

Example 5: Lignin Product Description

[0211] The posttreated biomass digestate from Example 4 were dried and the resulting dried posttreated biomass digestate was a lignin fraction comprising the following:

[0212] Lignin: 36%

[0213] Water content: 12%

[0214] Ash: 4.5%

[0215] Chlorine: 0.013%

[0216] Sulphur: 0.4%

[0217] Calorific value: 18. MJ/kg

Example 6

[0218] Biomass digestate may for example advantageously be provided by subjecting a soft biomass to heating in a non-pressurized pretreatment step at a pretreatment temperature between 65 to 100 degrees Celsius at ambient pressure. The heating may for example be performed in a tank or container with or without stirring. The retention time in the pretreatment step is usually short, such as less than one hour or less than 30 minutes, but it may also be longer if this may be convenient. The pretreated biomass may then be conveyed into a further tank to be anaerobic digested to provide a biomass digestate. The anaerobic digestion may be performed for example by the addition of bacteria. The anaerobic digestion is usually performed at a pH around neutral, such as for example between pH 6-8. An important degradation product, which may be obtained from the anaerobic digestion step is biogas, comprising methane and/or carbon dioxide.

Example 7: Removing Phosphorus from the Liquid Wash Fraction Using Base Precipitation

[0219] This example describes how to remove the phosphorus by addition of base from the liquid wash fraction obtained from the acidic wash step.

[0220] An acid wash step has been performed prior. The wash was made by mixing 5400 g of water with 15 g of acetic acid and adding 540 g of fiber (solid biomass digestate fraction produced from separating digestate from a biogas plant) with an incubation temperature of 50° C. and an incubation time of 24 hours. Afterwards the washed biomass digestate was separated into a solid wash fraction (fiber fraction) and liquid wash fraction, and the liquid wash fraction was treated.

[0221] Materials and Methods: [0222] Liquid wash fraction obtained from acid wash of solid biomass digestate fraction (type of wash is described above) [0223] Calcium hydroxide, Ca(OH).sub.2 (>96%, Chemsolute) [0224] Sodium hydroxide, NaOH (99.5%, Chemsolute)

[0225] The liquid wash fraction was divided into 4 samples as shown in the table. The content of phosphorus was measured using inductively coupled plasma method optical emission spectrometry (ICP-OES). The stated amounts (in weight percent of the liquid wash fraction) of solid calcium hydroxide or sodium hydroxide were added to the samples and stirred for 1 h at ambient temperature. The pH reached 8.9 in sample 1-3 and 8.7 in sample 4. The precipitation was removed by centrifugation and the phosphorus concentration in the base-treated liquid wash fraction was measured again using ICP.

[0226] Results:

[0227] It is possible to remove at least 98% of the phosphorus from the liquid wash fraction by increasing the pH value using a base such as for example calcium hydroxide or sodium hydroxide. Addition of more base would likely further increase the pH value as well as improve the phosphorus removal.

TABLE-US-00004 TABLE 3 Phosphorus removal using base precipitation. P conc. P conc. [mg/L] m [mg/L] Sample m(LW) before base m(Ca(OH).sub.2) (NaOH) wt % after base P conc. nr. [g] addition [g] [g] base addition reduction 1 1000 125 0.48 0.00 0.048% 2.7 98% 2 1000 125 0.48 0.00 0.048% 2.7 98% 3 1001 118 0.45 0.00 0.045% 2.6 98% 4 1000 118 0.00 034 0.034% 4.0 97%

FIGURE REFERENCES

[0228] DRY. Drying step [0229] BD. Biomass digestate [0230] SEP. Separation step [0231] LF. Liquid fraction [0232] SBD. Solid biomass digestate fraction [0233] AW. Acidic wash step [0234] WBD. Washed biomass digestate, [0235] LW. Liquid wash fraction [0236] SW. Solid wash fraction [0237] POST. Posttreating [0238] PSW. Posttreated solid wash fraction [0239] PRE. pretreating [0240] AD. Anaerobic digesting [0241] PBD. Posttreated biomass digestate [0242] IEX. ion exchange [0243] LPBD. Liquid posttreated biomass digestate fraction [0244] SPBD. Solid posttreated biomass digestate fraction [0245] DPBD. Dried posttreated biomass digestate [0246] LIG. Lignin [0247] DRY. Drying step [0248] BG. Biogas [0249] SB. Soft Biomass [0250] NIT. Nitrogen