Patent Application
20150225757
The invention relates to a process for increasing the yield of dextrose production from dextrose containing solution by membrane technology. The invention concerns the integration of a membrane process with an enzymatic treatment.
Starch hydrolysates rich in dextrose are primarily used as a raw material in the manufacture of crystalline dextrose. Starch hydrolysates rich in dextrose can be obtained through acid conversion of starch, combined acid-enzymatic conversion or multiple enzyme conversion of starch.
Starch hydrolysates rich in dextrose are usually obtained from starch during enzymatic starch hydrolysis process. A typical process comprises:
After saccharification, the starch hydrolysate contains high amounts of dextrose. Crystalline dextrose, having a purity above 90 w/w %, can be recovered by crystallisation of this hydrolysate. The by-product of this recovery process is the mother liquor. This mother-liquor is typically sold as a low quality product at reduced price to the feed industry. However, the mother liquor still contains high amounts of dextrose and dextrose oligomers. This high by-product formation negatively affects the efficiency of dextrose production and recovery processes. The dextrose recovery of conventional processes is unsatisfactory.
U.S. Pat. No. 5,869,297 discloses a membrane process to produce substantially pure dextrose, with purity well over the 99%, nanofiltering a glucose syrup containing about 95% dextrose and 5% di- and trisaccharides. Crosslinked aromatic polyamide membranes were used. It discloses glucose syrups having a solids content of about 80 to 97% by weight dextrose and at least 2% di- or trisaccharides.
U.S. Pat. No. 6,126,754 describes a process for the manufacture of a starch hydrolysate with high dextrose content.
WO2007/138167 describes the design of nanofiltration processes for the separation and recovery of sugars at low molecular weight from polysaccharides.
There is a need for an economically-competitive process to increase the yield of current dextrose production processes with a further twofold purpose: decreasing the amount of by-products and enhancing their quality to achieve a commercially attractive purity in dextrose.
The present invention relates to a process comprising membrane filtration of a dextrose containing solution and treatment of the retentate resulting from the filtration, with one or more glucoamylase and/or pulullanase enzyme.
The present invention further relates to the use of membrane filtration and enzyme treatment of the retentate to increase the dextrose recovery from a dextrose containing solution.
The present invention is further illustrated by the accompanying drawing (
The present invention relates to a process comprising membrane filtration of a dextrose containing solution, and treatment of the retentate resulting from the filtration, with one or more glucoamylase and/or pulullanase enzyme.
The process of the present invention can be implemented for example in a dextrose production process. Such process typically comprises starch hydrolysis through liquefaction and saccharification steps:
The dextrose containing solution is the feed to the membrane unit, and can be any solution which contains dextrose. The dextrose containing solution comprises from 1 to 99 weight/weight % of dextrose, measured on the dry substance of the solution (w/w % ds). The dextrose content can be from 5 to 90 w/w % ds, from 10 to 85 w/w % ds, from 15 to 80 w/w % ds, from 20 to 70 w/w % ds, from 30 to 60 w/w % ds or from 50 to 80 w/w % ds. The dextrose containing solution can have a dry substance of up to 70w/w %. Preferably the dextrose containing solution has a dry substance of from 10 to 60 w/w %, more preferably of from 20 to 50 w/w %, even more preferably of from 30 to 40 w/w %.
The dextrose containing solution, for the purpose of the present invention can be a saccharified starch milk, the mother liquor of a crystallisation step, the by-product of a chromatography separation step, an enzyme treated retentate or a mixture of two or more thereof.
The dextrose containing solution can be a saccharified starch milk, such as coming out of the saccharification step of a starch hydrolysis process. Such saccharified starch milk typically comprises from 90 to 99 w/w % ds of dextrose.
Dextrose can be recovered from a dextrose containing solution by any suitable method known in the art. Such dextrose recovery method yields dextrose and a by-product, generally in the form of a solution. The dextrose containing solution for the purpose of the present invention can be such by-product of a dextrose recovery step.
The dextrose recovery step preferably comprises a crystallisation. Crystallisation can be done by any suitable crystallisation method known in the art, such as for example batch or continuous crystallisation. After crystallisation, dextrose crystals are recovered by any suitable method known in the art, such as centrifugation, to yield crystalline dextrose and a by-product, called mother liquor. This mother liquor can thus be the dextrose containing solution for the purpose of the present invention. Typically, the mother liquor has a dry substance of from 30 to 60 w/w %. Typically, the mother liquor still comprises from 70 to 85 w/w % ds of dextrose, preferably from 75 to 83 w/w % ds of dextrose.
The dextrose recovery step can comprise recovery of dextrose from a dextrose containing solution by chromatography. Thus alternatively, the dextrose containing solution can be the by-product of such dextrose recovery by chromatography.
The by-product formed either after crystallisation or chromatography, usually still comprises high amounts of dextrose and starch hydrolysis products other than dextrose such as disaccharides, trisaccharides and oligosaccharides. Such by-product can also comprise the saccharification enzymes, originally present in the saccharified starch milk. In one embodiment, the enzyme originally present in the saccharified starch milk has been deactivated throughout the process. In another embodiment, the saccharification enzyme has not been deactivated throughout the process and remains active in the by-product.
Further, the dextrose containing solution can be refined before the nanofiltration (‘refined dextrose containing solution’). Purification can comprise removal of salts and/or protein by resin treatment such as to bring the conductivity of the dextrose containing solution below 50 μS/cm. Resin can be for example cation-anion system.
Filtration membranes can be classified by their porous vs. nonporous structure. Alternatively, membrane processes can be identified on the basis of the main driving force, such as pressure difference, concentration difference, etc. Pressure-driven membrane separation processes for liquid mixtures are reverse osmosis, nanofiltration, ultrafiltration and microfiltration. Membrane performances greatly depend on operative conditions of pressure, temperature, composition and pH, whereas the process efficiency is also affected by the fluid-dynamic conditions existing in the modules, by the configuration of the membrane filtration unit (single-pass, feed and bleed etc.) and the module arrangement can be relevant as well. Filtration membranes can be characterized by their cut-off value. Membrane cut-off value can either be expressed in terms of particle size (particle size cut-off value) or in terms of molecular weight (molecular weight cut-off value). The maximum value, either in particle size or in molecular weight that a particle can have in order to pass the filtration membrane determines the cut-off value of the filtration membrane. Filtration processes result in the production of a permeate and a retentate. The permeate comprises material having either a particle size or a molecular weight equal to or smaller than the cut-off value of the membrane. The retentate comprises material having either a particle size or a molecular weight greater than the cut-off value of the membrane.
Preferably, the membrane filtration of the present invention comprises nanofiltration; more preferably, the membrane filtration of the present invention is a nanofiltration.
Nanofiltration typically shows separation characteristics which are intermediate between reverse osmosis and ultrafiltation, with some overlap at lower and higher cut off values.
For the process of the present invention, the nanofiltration membrane has a cut-off value which allows passage of dextrose molecules into the permeate while retaining glucose polymer molecules such as disaccharides and trisaccharides into the retentate. Preferably, the nanofiltration membrane has molecular weight cut-off values in the range of from 100 to 400 Dalton, preferably from 200 to 300 Dalton, more preferably from 150 to 200 Dalton. Such membrane are for example commercialised by Koch Membrane Systems or General Electric-Power & Water, also known as Desal membranes. Thus the present invention relates to a process comprising nanofiltration of a dextrose containing solution and treatment of the retentate resulting from the filtration, with one or more glucoamylase and/or pulullanase enzyme, wherein the nanofiltration allows passage of dextrose molecules into the permeate while retaining glucose polymer molecules such as disaccharides and trisacharides into the retentate.
Suitable modules are in tubular and/or in spiral wound configuration, in order to prevent concentration polarization phenomena in the feed side. Spiral wound modules are preferable showing feed spacers in the range 30-70 mil, preferably in the range 30-50 mil, more preferably at 50. Suitable modules are for example Module KOCH-4720SR2-N1, Module KOCH-MPS34A2Z, Module GE-DK4040C1027 , Module GE-DL4040C1025, with GE-DL8040C being even more suitable.
Preferably, the nanofiltration is carried out under temperature condition of from 30° C. and 60° C., preferably about 50° C., and pressure conditions are preferably in the range of from 15 and 35 bar, more preferably 25 to 30, even more preferably about 30 bar. pH is preferably in the range of from 3.5 to 5, more preferably in the range of from 4.2 to 4.5.
The permeate has a dextrose purity which is higher than the dextrose purity of the dextrose containing solution. It preferably comprises from 80 to 99 w/w % ds, more preferably from 90 to 99 w/w % ds, even more preferably from 95 to 99 w/w % ds of dextrose (dextrose purity). In one embodiment, the dry substance of the permeate is from 10 to 40 w/w %, preferably from 20 to 35 w/w % The permeate can be further treated to recover the dextrose, for example by crystallisation. Alternatively, the permeate can be concentrated and either used as a dextrose syrup or as a raw material for crystallisation to produce crystalline dextrose powder, or for fructose production. Alternatively, the permeate can be concentrated and sent to a hydrogenation process for production of polyols.
The dextrose purity of the retentate can be from 1 to 99 w/w % ds, more preferably from 50 to 80 w/w % ds, even more preferably from 60 to 75 w/w % ds of dextrose. The dry substance of the retentate can be from 10 to 50 w/w %, it can be from 30 to 45 w/w %, it can be from 35 to 40 w/w %.
The present invention relates to a process comprising membrane filtration of a dextrose containing solution, and an enzyme treatment of the retentate with one or more glucoamylase and/or pulullanase enzyme.
The dextrose content of the retentate is increased through the action of the glucoamylase and/or pulullanase enzyme, converting the glucose oligomers present in the retentate into dextrose.
The enzyme treatment can be achieved in different ways. Fresh enzyme can be added to the dextrose containing solution once or several times during a continuous process. Said enzyme is retained by the filtration membrane. In this way the enzyme converts the recycled retentate.
In a preferred embodiment, the enzyme is immobilized and/or adsorbed on the filtration membrane itself.
In another preferred embodiment, the enzyme is immobilized and/or adsorbed on an fixed phase system like a resin through which the retentate passes. Suitable resins are for example anionic, macroporous or phenolic resins. Suitable phenolic resin is for example Duolite A 568. The fixed phase system is suitably placed subsequent to the filtration membrane.
The temperature is chosen to be in the optimal range for the enzyme. In the case of a glucoamylase, a suitable temperature range is of 50 to 65° C. The pH of the retentate depends on the enzyme used. It is preferably in the range of from 3.5 to 5, more preferably in the range of from 4.2 to 4.5.
During the enzymatic conversion the percentage of dextrose in the retentate may be adjusted by varying the contact time between the retentate and the enzyme, dry substance of the retentate and the temperature of the reaction.
Through the action of the glucoamylase and/or pulullanase enzyme, the dextrose content of the retentate is increased. Preferably, it reaches the dextrose content level of the dextrose containing solution.
The enzymatically treated retentate is recycled and is used as the dextrose containing solution or as part of the dextrose containing solution. It is thus passed through a filtration membrane, to yield a retentate and a permeate. This retentate can be treated with enzyme and recycled in turn. This recycling can be repeated as many times as needed, to finally recover substantially all dextrose from the dextrose containing solution. At least 30% of the retentate can be recycled, preferably at least 50%, more preferably at least 70%, even more preferably at least 90% and most preferably 100% of the retentate is recycled. Thereby, the by-product formation of the dextrose production process is significantly decreased in amount and can even be eliminated. Thus in a most preferred embodiment, the process has one inflow stream, the dextrose containing solution, and one outflow stream, the permeate, while the retentate is recycled. The present invention allows to achieve yield of at least 80%, preferably at least 90%, more preferably at least 95%. It is understood that the yield for the purpose of the present invention is the ratio between the dry matter of the permeate on the dry matter of the dextrose containing solution.
Thus in the process of the present invention the dry substance of the permeate is at least 80%, preferably at least 90%, more preferably at least 95% of the dry substance of the dextrose containing solution.
Additonally, after the enzymatic treatment, the retentate can be demineralised with resin columns for example in order to remove ionic content and proteins. The demineralised, enzymatically treated retentate is then recycled to the membrane filtration.
The process of the present invention can be batch, continuous or semi-continuous.
The invention most preferably relates to a process comprising the following steps:
The present invention also allows working with dextrose containing solution having a high dry substance content. In conventional processes, nanofiltration requires that the incoming dextrose containing solution has a dry substance content of up to 10 to 25 w/w %. At higher dry substance contents, a lot of retentate is produced which means a lot of low quality by-product to be sold at lower price. With the present invention, there is no loss of retentate, there is limited to no by-product formation, because of the recycling of the retentate to the filtration unit. Therefore dextrose containing solution having a dry substance of up to 70 w/w % can be used. Conveniently, the dextrose containing solution has a dry substance content of from 20 w/w % to 60 w/w %.
Further, the present invention relates to a use of membrane filtration and enzyme treatment of the retentate to increase dextrose recovery from a dextrose containing solution. Membrane filtration, dextrose containing solution and enzyme treatment are as described above. In conventional processes, dextrose recovery is about 50%. With the process of the present invention, dextrose recovery is greater than 95%.
A pilot system (
This example describes a continuous nanofiltration process of mother liquor coming from the centrifugation of dextrose crystallization process. The example is schematically represented in
Nanofiltration (8) is carried out at 50° C., at pH values of 4 and feed pressure conditions of 30 bar. Spiral wound thin film composite membranes Desal GE-DL4040C 1025 are used, manufactured by General Electric; general specifications are reported in the following table
The nanofiltration unit operates with a minimum overall volume concentration factor of 2.2 with a surface of 125 m2/tons of diluted mother liquor.
0.39 tons/h of mother liquor coming from the centrifugation of dextrose crystallization process (1), at 50 w/w % dry substance (weight/weight %) and 82 w/w % dextrose purity, is refined (de-ashing) in a double pass resin system (cation-anion) (2) to remove salts and proteins. The mother liquor after refining has a conductivity below 50 μS/cm (refined mother liquor (3)).
0.033 tons/h of refined mother liquor (5) is mixed with 0.56 tons/h of upgraded retentate (11) coming from the enzyme treatment and having a dry substance of 39 w/w % and a dextrose purity of 82 w/w %. This provides 0.89 tons/h of diluted mother liquor (6). The 0.89 tons/h of diluted mother liquor is further diluted with 0.39 tons/h of water (7) in a feed tank in order to obtain 1.28 tons/h of further diluted mother liquor at a dry substance of 30 w/w %. The latter is fed to the nanofiltration unit (8). The permeate stream (P) (0.7 tons/h) has a dry substance of 23 w/w %, and a dextrose purity of 98 w/w % and is mixed with 0.06 Tons/h of the refined mother liquor (4) to yield a syrup having a dry substance of 24.8 w/w % and a dextrose purity of 97.3 w/w %. This syrup is pumped to the crystallization monohydrate process.
The retentate (R) (0.58 tons/h) has a dry substance of 39 w/w %, and a dextrose purity of 71.5 w/w %. The retentate is fed to a column Duolite568 with bound glucoamylase and pullulanase enzyme in order to convert the polysaccharides into dextrose to increase the dextrose purity level at same level than the nanofiltration feed solution, i.e. 82 w/w % (‘upgraded retentate’ (9)). Conversion occurs within one hour retention time at pH 4-5, at 50° C.
0.56 tons/h of upgraded retentate (11) is recycled to the nanofiltration unit as explained above, and 0.022 t/h of the upgraded retentate (10) is sent to the concentrator for downstream utilization.
The example described allows achieving an overall yield of at least 95% tons ds of permeate (P) liquor/tons ds of mother liquor coming from crystallization (1).
| Number | Date | Country | Kind |
|---|---|---|---|
| 12006676.6 | Sep 2012 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/US2013/060865 | 9/20/2013 | WO | 00 |
