The invention relates to a process for the preparation of a fermentation product from lignocellulosic material, comprising the following steps: a) optionally, pretreatment of the lignocellulosic material, b) optionally, washing of the optionally pretreated lignocellulosic material, c) enzymatic hydrolysis of the optionally washed and/or optionally pretreated lignocellulosic material using an enzyme composition comprising at least two cellulases and whereby the enzyme composition at least comprises LPMO, and optionally purifying the hydrolysed lignocellulosic material, d) fermentation of the hydrolysed lignocellulosic material to produce a fermentation product, and e) optionally, recovery of a fermentation product, wherein the amounts of formed hydrolysed oxidation products at the end of the enzymatic hydrolysis by the oxidation by LPMO of the lignocellulosic material containing cellulose and/or cello-oligosaccharides is kept between 3 to 80 g/kg glucan present in the lignocellulosic material by adding a suitable amount of oxygen after the pre-treatment and before and/or during the enzymatic hydrolysis to the lignocellulosic material, preferably the formed hydrolysed oxidation product is gluconic acid, an aldonic acid and/or geminal diol, more preferably the hydrolysed oxidation product is gluconic acid.

The invention relates to a process for the preparation of a fermentation product from lignocellulosic material, comprising the following steps: a) optionally, pretreatment of the lignocellulosic material, b) optionally, washing of the optionally pretreated lignocellulosic material, c) enzymatic hydrolysis of the optionally washed and/or optionally pretreated lignocellulosic material using an enzyme composition comprising at least two cellulases and whereby the enzyme composition at least comprises LPMO, and optionally purifying the hydrolysed lignocellulosic material, d) fermentation of the hydrolysed lignocellulosic material to produce a fermentation product, and e) optionally, recovery of a fermentation product, wherein the amounts of formed hydrolysed oxidation products at the end of the enzymatic hydrolysis by the oxidation by LPMO of the lignocellulosic material containing cellulose and/or cello-oligosaccharides is kept between 3 to 80 g/kg glucan present in the lignocellulosic material by adding a suitable amount of oxygen after the pre-treatment and before and/or during the enzymatic hydrolysis to the lignocellulosic material, preferably the formed hydrolysed oxidation product is gluconic acid, an aldonic acid and/or geminal diol, more preferably the hydrolysed oxidation product is gluconic acid.

A process for hydrolyzing at least part of the hemicellulose and at least part of the cellulose of a particulate solid material comprising cellulose, lignin, and from 10 to 60% by weight of hemicellulose, wherein said hemicellulose comprises xylose in an amount of from 40 to 100% by weight, on the basis of hemicellulose, said process being conducted in at least one reactor comprising said particulate solid material and interstitial space. The process comprises two hydrolysis steps using hydrochloric acid, separated by a displacement step wherein a water-immiscible displacement fluid displaces part of the hydrochloric acid containing hydrolysate products from the interstitial space in the reactor. In the present process, a particulate solid material is used of which the hemicellulose is high in xylose (xylan).

A process for hydrolyzing at least part of the hemicellulose and at least part of the cellulose of a particulate solid material comprising cellulose, lignin, and from 10 to 60% by weight of hemicellulose, wherein said hemicellulose comprises xylose in an amount of from 40 to 100% by weight, on the basis of hemicellulose, said process being conducted in at least one reactor comprising said particulate solid material and interstitial space. The process comprises two hydrolysis steps using hydrochloric acid, separated by a displacement step wherein a water-immiscible displacement fluid displaces part of the hydrochloric acid containing hydrolysate products from the interstitial space in the reactor. In the present process, a particulate solid material is used of which the hemicellulose is high in xylose (xylan).

Non-dried allulose crystals are dried in a temperature treating step (b) in a drying apparatus at a temperature of about 25° C. to about 70° C., and in a conditioning step (c). The temperature treating step (b) may be carried out (b1) at atmospheric pressure and a residence time of about 5 minutes to about 5 hours. The temperature treating step (b) may be carried out (b2) under reduced pressure and constant temperature and a residence time from about 40 minutes to about 5 hours. The conditioning step (c) may be carried out (c1) over a period of about 30 minutes to 7 hours at a temperature from about 40° C. to about 70° C. The conditioning step (c) may be carried out (c2) over a period of about 15 minutes to about 90 hours at about 30 to about 60% relative humidity, and a temperature of about 25 to about 40° C.

Non-dried allulose crystals are dried in a temperature treating step (b) in a drying apparatus at a temperature of about 25° C. to about 70° C., and in a conditioning step (c). The temperature treating step (b) may be carried out (b1) at atmospheric pressure and a residence time of about 5 minutes to about 5 hours. The temperature treating step (b) may be carried out (b2) under reduced pressure and constant temperature and a residence time from about 40 minutes to about 5 hours. The conditioning step (c) may be carried out (c1) over a period of about 30 minutes to 7 hours at a temperature from about 40° C. to about 70° C. The conditioning step (c) may be carried out (c2) over a period of about 15 minutes to about 90 hours at about 30 to about 60% relative humidity, and a temperature of about 25 to about 40° C.

Related to are a device and a method for performing continuous carbonation and impurity removal for xylose mother liquor. The device includes an alkali addition unit, a continuous carbonating unit, a discharge controlling unit, a CO.sub.2 supply station, a vapor station and an after-carbonation tank, wherein the alkali addition unit is configured to add Ca(OH).sub.2 alkaline liquid into xylose mother liquor, the continuous carbonating unit is configured to introduce CO.sub.2 supplied from the CO.sub.2 supply station into the alkali-added xylose mother liquor to perform carbonation and mixing so as to remove impurities such as colloid and pigment in xylose mother liquor, the discharge controlling unit is configured to introduce CO.sub.2 supplied from the CO.sub.2 supply station and vapor transported from the vapor station into the carbonated xylose mother liquor so as to control and stabilize a pH value of the carbonated xylose mother liquor, and the after-carbonation tank is configured to collect and temporarily store the carbonated and impurity-removed xylose mother liquor so as to prepare for a next procedure. Further, a method using the device is disclosed. According to the device and the method, the pH of xylose mother liquor is continuously regulated and stabilized and continuous feeding and discharge are performed with highly automated device so as to achieve continuous and uninterrupted production, and thus facilitate improving the production efficiency.

The teachings herein relate to a process for drying allulose crystals. The process includes a step of providing non-dried allulose crystals. The process includes temperature treating the crystals at a temperature in the range of about 25 to about 70° C. in a drying apparatus to form an intermediate product. The process includes conditioning the intermediate process. The conditioning may be for about 30 minutes to 7 hours at 40 to 70° C. The conditioning may be for about 15 to about 90 hours with air of a relative humidity of about 30 to about 60% at 25 to about 40° C.

The teachings herein relate to a process for drying allulose crystals. The process includes a step of providing non-dried allulose crystals. The process includes temperature treating the crystals at a temperature in the range of about 25 to about 70° C. in a drying apparatus to form an intermediate product. The process includes conditioning the intermediate process. The conditioning may be for about 30 minutes to 7 hours at 40 to 70° C. The conditioning may be for about 15 to about 90 hours with air of a relative humidity of about 30 to about 60% at 25 to about 40° C.

Disclosed herein are methods, systems, and compositions for the uniform pretreatment of biomass within seconds with low inhibitor formation. The pretreatment process is used to convert biomass to a fuel, sugars, or other useful chemicals by subjecting the feedstock to a rapid retention time under pressure and temperature and/or chemical reactant. The system includes at least one high pressure, steam impermiable plug and a continuously-operating valve discharge apparatus to discharge pretreated feedstock while maintaining uniform pressure on the pretreatment system.