Classifications

• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23L—FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES, NOT OTHERWISE PROVIDED FOR; PREPARATION OR TREATMENT THEREOF
  • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Preparation or treatment thereof
  • A23L2/02—Non-alcoholic beverages; Dry compositions or concentrates therefor; Preparation or treatment thereof containing fruit or vegetable juices
  • A23L2/08—Concentrating or drying of juices
  • A23L2/082—Concentrating or drying of juices by membrane processes
• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; PREPARATION THEREOF
  • A23C9/00—Milk preparations; Milk powder or milk powder preparations
  • A23C9/14—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment
  • A23C9/142—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by dialysis, reverse osmosis or ultrafiltration
  • A23C9/1422—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by dialysis, reverse osmosis or ultrafiltration by ultrafiltration, microfiltration or diafiltration of milk, e.g. for separating protein and lactose; Treatment of the UF permeate
• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23L—FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES, NOT OTHERWISE PROVIDED FOR; PREPARATION OR TREATMENT THEREOF
  • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Preparation or treatment thereof
  • A23L2/02—Non-alcoholic beverages; Dry compositions or concentrates therefor; Preparation or treatment thereof containing fruit or vegetable juices
  • A23L2/08—Concentrating or drying of juices
  • A23L2/082—Concentrating or drying of juices by membrane processes
  • A23L2/087—Concentrating or drying of juices by membrane processes by ultrafiltration, microfiltration
• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23L—FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES, NOT OTHERWISE PROVIDED FOR; PREPARATION OR TREATMENT THEREOF
  • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Preparation or treatment thereof
  • A23L2/385—Concentrates of non-alcoholic beverages
• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23L—FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES, NOT OTHERWISE PROVIDED FOR; PREPARATION OR TREATMENT THEREOF
  • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Preparation or treatment thereof
  • A23L2/52—Adding ingredients
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
  • B01D61/027—Nanofiltration
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/14—Ultrafiltration; Microfiltration
  • B01D61/145—Ultrafiltration
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/58—Multistep processes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
  • B01D71/02—Inorganic material
  • B01D71/028—Molecular sieves
• • C—CHEMISTRY; METALLURGY
  • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
  • C12C—BEER; PREPARATION OF BEER BY FERMENTATION; PREPARATION OF MALT FOR MAKING BEER; PREPARATION OF HOPS FOR MAKING BEER
  • C12C12/00—Processes specially adapted for making special kinds of beer
  • C12C12/02—Beer with low calorie content
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2311/00—Details relating to membrane separation process operations and control
  • B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2311/00—Details relating to membrane separation process operations and control
  • B01D2311/06—Specific process operations in the permeate stream
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2311/00—Details relating to membrane separation process operations and control
  • B01D2311/08—Specific process operations in the concentrate stream
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2311/00—Details relating to membrane separation process operations and control
  • B01D2311/26—Further operations combined with membrane separation processes
  • B01D2311/2626—Absorption or adsorption
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2311/00—Details relating to membrane separation process operations and control
  • B01D2311/26—Further operations combined with membrane separation processes
  • B01D2311/2688—Biological processes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2311/00—Details relating to membrane separation process operations and control
  • B01D2311/26—Further operations combined with membrane separation processes
  • B01D2311/2699—Drying
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2315/00—Details relating to the membrane module operation
  • B01D2315/10—Cross-flow filtration

Definitions

• the present disclosure generally relates to methods and systems for the preparation of beverages having reduced sugar content.
• High caloric intake is well-known for being associated with various concerns, such as weight gain and related health problems.
• consumers are becoming increasingly health- and weight-conscious, and the calorie capacity of foods and beverages is becoming a very significant consideration.
• Food and beverage manufacturers are marketing health and wellness products having lower calorie contents, in order to attract such consumers.
• low-calorie foods and beverages tend to lack flavor due to low perceived sweetness. Manufacturers have tried to address this issue by adding high amounts of artificial sweeteners and flavoring agents.
• low-calorie orange juice is produced by diluting reduced sugar orange juice and adding large quantities of artificial sweeteners, coloring and flavorings agents to make it resemble natural orange juice.
• certain artificial ingredients are inherently not natural and believed to cause serious health problems. Therefore, most of the known artificially sweetened juices and/or other beverages including milk and beer are not well-received by consumers. This is particularly true with low-calorie beverages.
• US 5,403,604 relates to a process for separating sugars from a fruit juice to form a high Brix/acid (B/A) ratio fruit juice fraction and a low Brix/acid (B/A) ratio fruit juice fraction.
• This process comprises: (a) passing a fruit juice through an ultrafiltration (UF) membrane to form: (i) a UF retentate comprising water, cloud, oil soluble flavors, oil soluble colors and pulp, and (ii) an UF permeate; (b) passing the UF permeate from step (a) through a nanofiltration (NF) membrane that has a low permeability to fruit juice sugars to form (i) an NF retentate having a high sugar content and (ii) an NF permeate having a low sugar content; (c) optionally concentrating the NF permeate to remove water: (d) optionally recirculating the removed water from step (c) to any other step in said process; (e) adding a portion of the UF retentate from step (a) to the high sugar content NF retentate of step (b) to form a high B/A ratio fruit juice fraction; and (f) adding a portion of the UF retentate from step (a) to the low sugar content
• US 9,220,291 is directed to a method for producing a juice product.
• the method of US 9,220,29 comprises: providing a juice; processing the juice to selectively remove more sucrose than monosaccharides to produce a stream of clarified low-calorie juice; and producing a juice product from the clarified low-calorie juice, wherein sugar content of the juice product comprises 0 to 30% sucrose w/w, and wherein the juice product contains no artificial sweeteners.
• US 2011/165310 discloses a method for treating a sugar-containing natural consumable product for lowering its sugar content.
• the method disclosed in US 2011/165310 includes the steps of: (a) passing a stream of a sugar-containing natural consumable product into contact with a bed of material capable of chromatographically separating sugar from the natural consumable product; and (b) chromatographically separating a sugar-diminished natural consumable product from the bed.
• WO 2014/161998 is directed to a process for reducing the alcohol content and/or the sugar content of a beverage, said process comprising the steps of: a. contacting the beverage with a particulate porous adsorbent material; and b. separating the beverage from the particulate porous adsorbent material; the particles of the porous adsorbent material having been treated externally with a hydrophobic coating.
• WO 2019/106564 discloses a method of lowering the sugar content of beverages, which comprises: contacting a first adsorbent with a beverage, the first adsorbent being active so as to have selectivity for polysaccharides, to treat the beverage and obtain a treated beverage; hydrolyzing the polysaccharides bound to the first adsorbent into monosaccharides after the beverage has contacted the first adsorbent; and, washing the first adsorbent with a solution to remove the hydrolyzed monosaccharides.
• WO 2020/064973 relates to a method for producing orange juice.
• the method comprises ultra-filtering raw orange juice to produce an ultra-filtered permeate and an ultra-filtered retentate, nano-filtering the ultra-filtered permeate to produce a nanofiltered permeate and a nano-filtered retentate, mixing the ultra-filtered retentate and the nano-filtered permeate to produce orange juice having a sugar content in the interval 67% to 77% of the sugar content of the raw orange juice, pasteurizing the orange juice, and aseptically filling packets with the orange juice produced by the mixing.
• WO 2021/220131 discloses an aromatic water drink obtained from a fruit juice comprising a reduced Brix degree of at least 50% compared to the fruit juice.
• the aromatic water drink of WO 2021/220131 is produced following the steps of: providing a fruit juice, performing a nanofiltration of said fruit juice or adjusted fruit juice through a nanofiltration membrane; and recovering the permeate water from said nanofiltration to obtain the aromatic water drink, wherein the permeate water has a reduced Brix degree by at least 50% compared to the fruit juice.
• GB 2407573 relates to a process of recovering arabinose and optionally at least one other monosaccharide from vegetable fiber rich in heteropolymeric arabinose.
• the process of GB 2407573 comprises the following steps: (a) controlled hydrolysis of vegetable fiber in an aqueous solution to produce an aqueous hydrolyzate containing arabinose, at least one other monosaccharide and optionally poly-, oligo- and/or disaccharides, (b) optional neutralization of said aqueous hydrolyzate, followed by at least one of the following steps (c) and (d): (c) fractionation of said aqueous hydrolyzate to obtain a fraction enriched in arabinose, at least one other sugar fraction (d) crystallization of arabinose.
• the present invention provides improved processes for treating beverages. Specifically, the invention provides system and methods for reducing the sugar content of a beverage including fruit or vegetable juice, milk or beer and for isolating a sugar fraction from the beverage, which may be further employed in the industry.
• a system for reducing the sugar content of a beverage comprising: (i) at least one ultrafiltration (UF) unit comprising: a housing defining an inner UF chamber fluidly coupled to a UF inlet port, a UF permeate outlet port, and a UF retentate outlet port; and at least one UF filter disposed within the UF housing; (ii) at least one nanofiltration (NF) unit comprising: a housing defining an inner NF chamber, wherein the inner NF chamber is fluidly coupled to an NF inlet port, which is fluidly coupled to the UF permeate outlet port, wherein the inner NF chamber is further fluidly coupled to a NF permeate outlet port and to an NF retentate outlet port; and at least one NF filter disposed within the inner NF chamber; (iii) a liquid pump configured to pump the ultrafiltered permeate from the inner UF chamber to the inner NF chamber through the UF permeate outlet port
• the beverage can be a fruit or vegetable juice, milk, beer, or any other sugar containing beverage whereas one or more operational parameters of the system can be adjusted for example according to the beverage to be treated and/or according to the desired characteristics of the resultant treated beverage.
• the liquid pump is configured to facilitate the nano-filtering of the ultra-filtered permeate through the at least one NF filter, at a TMP of 10 to 65 Bar. In some embodiments, the liquid pump is configured to facilitate the nano-filtering of the ultra-filtered permeate through the at least one NF filter, at a TMP of 10 to 20 Bar, 10 to 30 Bar, 10 to 40 Bar, 10 to 50 Bar, 10 to 60 Bar, 10 to 65 Bar, 15 to 25 Bar, 20 to 30 Bar, 25 to 35 Bar, 30 to 40 Bar, 35 to 45 Bar, 40 to 50 Bar, 45 to 55 Bar, 50 to 60 Bar, or 55 to 65 Bar.
• TMP 10 to 20 Bar, 10 to 30 Bar, 10 to 40 Bar, 10 to 50 Bar, 10 to 60 Bar, 10 to 65 Bar, 15 to 25 Bar, 20 to 30 Bar, 25 to 35 Bar, 30 to 40 Bar, 35 to 45 Bar, 40 to 50 Bar, 45 to 55 Bar, 50 to 60 Bar, or 55 to 65 Bar.
• the system further comprises a controller for increasing the TMP during at least a part of the nanofiltration.
• the controller can be the same controller that controls all the operations of the system.
• the controller can be a specific controller for controlling the TMP.
• the controller controls or regulates (for example, increases) the TMP by controlling the liquid pump.
• the controller controls or regulates (for example, increases) the TMP by controlling the opening / closing and/or open/close extent of a valve or by controlling other components effecting the TMP.
• the controller increases the TMP continuously.
• the controller increases the TMP periodically or in discrete steps.
• the controller can be a pre-programmed controller to automatically regulate the TMP according to a predetermined pattern.
• At least one of the UF filtration unit and the NF filtration unit comprises a crossflow filtration unit.
• the system further comprises at least one adsorption unit comprising: a housing in the form of an elongated tube column, which is defining an inner adsorption chamber, which contains at least one adsorbent disposed therein, wherein the at least one adsorbent comprises a zeolite, and is active so as to have a higher relative selectivity for disaccharides than for monosaccharides and, optionally, for organic acids; and an adsorption unit inlet port fluidly coupled with the NF permeate outlet port.
• the NF inlet port is connected to the UF permeate outlet port though a UF-NF pipe; and the adsorption unit inlet port is connected to the NF permeate outlet port though a NF-adsorbent pipe.
• the liquid pump is configured to pump the nano-filtered permeate from the inner NF chamber to the inner adsorption chamber through the NF permeate outlet port and the adsorption unit inlet port.
• the same liquid pump can be used to pump the nanofiltered permeate.
• the system can comprise an additional (booster) pump to pump the NF permeate.
• the system further comprises a treated beverage container in fluid communication with the treated beverage outlet port, wherein the pump is further configured to pump the treated beverage from the inner adsorption chamber into the treated beverage container through the treated beverage outlet port.
• the pump is configured to pump the NF permeate as the treated beverage from the NF unit into the treated beverage container through the treated beverage outlet port for example via an adsorption bypass line.
• the UF retentate outlet port is connected to the treated beverage container through a UF-container pipe, and wherein the pump is further configured to pump the UF retentate to the treated beverage container using the pump.
• the system further comprises at least one centrifugation unit comprising: a housing defining an inner centrifugation chamber, wherein the inner centrifugation chamber is fluidly coupled to a centrifugation inlet port, wherein the inner centrifugation chamber is further fluidly coupled to a centrifuged aqueous medium outlet port and to centrifuged solid outlet port, wherein the centrifuged aqueous medium outlet port is fluidly coupled with the UF inlet port; and a centrifuge disposed within the inner centrifugation chamber; wherein the pump is configured to pump the aqueous medium from the inner centrifugation chamber to the inner UF chamber through the aqueous medium outlet port and the UF inlet port.
• the centrifuged aqueous medium outlet port is connected to the UF inlet port through a centrifuge-UF pipe.
• the centrifuged solid outlet port is connected to the treated beverage container.
• the centrifugation unit may not be used and the beverage to be treated can be fed directly into the UF unit.
• the adsorption unit may not be used and the NF permeate can be directly fed from the NF unit to the treated beverage container.
• the UF retentate and/or solids from the centrifugation unit may not be fed to the treated beverage container.
• the UF filter has molecular weight cutoff in the range of 5-20 kDa and the NF filter has molecular weight cutoff in the range of 150-500 Da.
• At least one of the UF filtration unit and the NF filtration unit comprises a crossflow filtration unit.
• either or both of the ultrafiltration and nanofiltration is performed using crossflow filtration technique.
• at least the nanofiltration is performed using crossflow filtration technique.
• the invention further provides methods for reducing the sugar content of a beverage and for isolating a sugar fraction from the beverage.
• the present method includes an optional (based on the beverage and/or the desired result) initial step of performing a solid separation step, e.g., a centrifugation, for removing insoluble solid components, such as pulp, for example in the embodiments in which the beverage is a fruit or vegetable juice, so that the next step may be conducted easily, according to some embodiments.
• the method includes ultra-filtering (UF) the beverage to produce a UF retentate and an UF permeate, which is then being nano-filtered (NF) to produce a NF permeate and a NF retentate, according to some embodiments.
• UF ultra-filtering
• NF nano-filtered
• the NF retentate is isolated and dried to produce a sugar composition according to the present invention, according to some embodiments, and the NF permeate is then optionally subjected to a zeolite adsorption and filtered.
• an additive such as the UF retentate and/or a flavoring agent, is then added to the nano-filtered retentate or to the adsorption filtrate.
• the nano-filtered permeate of step (c), the adsorption filtrate of step (d) or the addition product is then isolated to provide a reduced sugar beverage, according to some embodiments, advantageously, the method of the present invention reduced at least 30% of the total sugars and at least 80% of the sucrose from the beverage, while maintaining nutritional compounds.
• the present invention provides a method of reducing the sugar content of a beverage, the method comprising: (a) providing a beverage; (b) ultra-filtering the beverage through an ultrafiltration membrane, which has molecular weight cutoff in the range of 5-20 kDa to produce an ultra-filtered permeate and an ultra-filtered retentate; and (c) nano-filtering the ultra-filtered permeate through a nanofiltration membrane, at a TMP (Trans Membrane Pressure) of at least 10 Bar, wherein the nanofiltration membrane has molecular weight cutoff in the range of 150-500 Da to produce a nano-filtered permeate and a nano-filtered retentate.
• TMP Trans Membrane Pressure
• the method comprises nano-filtering the ultrafiltered permeate through the nanofiltration membrane, at a TMP of 10 to 65 Bar. In some embodiments, the method comprises nano-filtering the ultra-filtered permeate through the nanofiltration membrane, at a TMP of 10 to 20 Bar, 10 to 30 Bar, 10 to 40 Bar, 10 to 50 Bar, 10 to 60 Bar, 10 to 65 Bar, 15 to 25 Bar, 20 to 30 Bar, 25 to 35 Bar, 30 to 40 Bar, 35 to 45 Bar, 40 to 50 Bar, 45 to 55 Bar, 50 to 60 Bar, or 55 to 65 Bar.
• TMP 10 to 20 Bar, 10 to 30 Bar, 10 to 40 Bar, 10 to 50 Bar, 10 to 60 Bar, 10 to 65 Bar, 15 to 25 Bar, 20 to 30 Bar, 25 to 35 Bar, 30 to 40 Bar, 35 to 45 Bar, 40 to 50 Bar, 45 to 55 Bar, 50 to 60 Bar, or 55 to 65 Bar.
• the method further comprises increasing the TMP during at least a part of step (c).
• the TMP can be controlled by the controller described above.
• the TMP can be controlled by controlling a pump facilitating the TMP.
• the TMP can be controlled by controlling one or more valves or other components effecting the TMP.
• the TMP can be increased continuously.
• the TMP can be increased periodically or in discrete steps.
• the TMP can be increased according to a predetermined pattern.
• the present invention provides a method of reducing the sugar content of a beverage, the method comprising: (a) providing a beverage; (b) ultra-filtering the beverage through an ultrafiltration membrane, which has molecular weight cutoff in the range of 5-20 kDa to produce an ultra-filtered permeate and an ultra-filtered retentate; (c) nano-filtering the ultra-filtered permeate through a nanofiltration membrane, which has molecular weight cutoff in the range of 150-500 Da to produce a nano-filtered permeate and a nano-filtered retentate; (d) contacting at least one adsorbent with the nano-filtered permeate to produce an adsorbed composition and a liquid medium, and filtering the adsorbed composition from liquid medium to form an adsorption filtrate, wherein the at least one adsorbent comprises a zeolite, and wherein the at least one adsorbent has a higher relative selectivity for disaccharides than for monosaccharides and, optionally
• the method further comprises step (e). According to some embodiments, the method further comprises step (e), wherein the additive comprises the ultra-filtered retentate of step (b).
• the beverage is a fruit or vegetable juice and the ultra-filtered retentate comprises vitamin C. According to some embodiments, the beverage is a fruit or vegetable juice and the ultra-filtered retentate comprises 0.1 to 50 mg/ 100 ml vitamin C.
• the beverage is a fruit or vegetable juice and the fruit or vegetable juice is a fruit juice and the isolated treated beverage product is an isolated treated fruit juice product.
• the beverage is a fruit juice and the fruit juice is a citrus fruit juice and the isolated treated fruit juice product is a reduced-sugar citrus fruit juice.
• the citrus fruit juice is selected from the group consisting of orange juice, grapefruit juice, clementine juice, mandarine juice and combinations thereof. Each possibility represents a separate embodiment of the invention.
• step (b) comprises ultra-filtering the beverage through an ultrafiltration membrane, which has molecular weight cutoff in the range of 5-20 kDa.
• step (c) comprises nano-filtering the ultrafiltered permeate through a nanofiltration membrane, which has molecular weight cutoff in the range of 180-500 Da.
• step (c) comprises nano-filtering the ultra-filtered permeate through a nanofiltration membrane, which has molecular weight cutoff in the range of 300-500 Da, including each value and subrange within the specified range.
• step (c) comprises nano-filtering the ultra-filtered permeate through a nanofiltration membrane, at a TMP (Trans Membrane Pressure) of at least 10 Bar.
• TMP Trans Membrane Pressure
• the TMP is in the range of 10 to 40 Bar.
• At least one of the ultra-filtering and the nanofiltering comprises crossflow filtering. According to some embodiments, either or both of the ultrafiltration and nanofiltration is performed using crossflow filtration technique. According to some embodiments, at least the nanofiltration is performed using crossflow filtration technique.
• the beverage provided in step (a) comprises insoluble solid dispersed in an aqueous medium, and wherein step (b) comprises separating at least part of the insoluble solids from the beverage through the ultrafiltration.
• the beverage is a fruit or vegetable juice and the fruit or vegetable juice is a fruit juice, wherein the insoluble solids comprise fruit juice pulp, and wherein step (b) comprises separating at least part of the pulp from the aqueous medium.
• the beverage is a fruit or vegetable juice and the disaccharides comprise sucrose, and the monosaccharides comprise fructose, glucose or a combination thereof.
• the disaccharides comprise sucrose
• the monosaccharides comprise fructose, glucose or a combination thereof.
• the beverage is a fruit or vegetable juice and the isolated treated juice has a ratio of sucrose to total sugars below 70% w/w. According to some embodiments, the treated juice has a ratio of sucrose to total sugars of about 30%-60%.
• the method comprises step (d).
• step (d) comprises passing the nano-filtered permeate though a column comprising the at least one adsorbent to produce an adsorbed composition within the column and an adsorption filtrate exiting the column.
• the zeolite is selected from zeolites having a
• the zeolite comprises at least one of Y Zeolite H + and Y Zeolite Ca.
• the beverage is a fruit or vegetable juice and the method comprises step (e), wherein the additive comprises an untreated fruit or vegetable juice.
• the beverage is a fruit or vegetable juice and the fruit or vegetable juice provided in step (a) has an initial Brix/acidity ratio, and the isolated treated fruit or vegetable juice has a treated Brix/acidity ratio which is at least 10% lower than the initial Brix/acidity ratio.
• the beverage is a fruit juice and the isolated NF Permeate comprises 50% to 80% less sucrose than the untreated fruit juice prior to step (a).
• the isolated treated fruit juice product comprises at least 30% less sugar than the untreated fruit juice prior to step (a).
• the beverage is a fruit or vegetable juice and the isolated treated fruit or vegetable juice product comprises 50% to 80% less sucrose than the untreated fruit or vegetable juice provided in step (a).
• the isolated treated fruit or vegetable juice product comprises at least 50% less sucrose than the untreated fruit or vegetable juice provided in step (a).
• the phrase “50% less sucrose” and similar embodiments means that per volume unit the weight of the sucrose is reduced by 50% or more through the method. Thus, if a starting beverage has total sucrose concentration of 8 gr/ml, the isolated treated beverage will have total sucrose concentration of 4 gr/ml or less.
• the method comprises step (e) wherein the additive is selected from the group consisting of: a taste masking agents, a sweetener, a preservative or any combination thereof.
• the taste masking agent comprises a natural extract selected from the group consisting of: cinnamon, chocolate, vanilla, strawberry, coconut, ginger, licorice and a combination thereof.
• the sweetener is a carbohydrate or proteinbased sweetener.
• the sweetener is selected from the group consisting of: date, Stevia, agave fruit, honey, apple, Erythritol, Sweetango, maple, and a combination thereof.
• the sweetener comprises Incredo (Douxmatok), sweelinTM (Amai), or both.
• the beverage is milk.
• the beverage has total sugars including disaccharides comprising lactose.
• the treated milk comprises at least 50% less lactose than the untreated milk provided in step (a).
• the treated milk has 50% to 90% less lactose than the untreated milk, including each value and sub-range within the specified range.
• the treated milk has 80% less lactose than the untreated milk.
• the milk contains calcium, protein, along with other minerals and vitamins.
• the untreated milk comprises 4.7 g lactose per 100 g of milk.
• the untreated milk has brix in the range of 5% to 15%, including each value and sub-range within the specified range.
• the treated milk has brix in the range of 4% to 8%, including each value and sub-range within the specified range.
• Each possibility represents a separate embodiment of the invention.
• the beverage is beer.
• the beverage has total sugars including disaccharides comprising maltose, and monosaccharides comprising glucose.
• the treated beer comprises at least 30% less total sugars than the untreated beer provided in step (a).
• the treated beer has 30% to 80% less total sugars than the untreated beer, including each value and sub-range within the specified range.
• the beer which is to treated by the present method may include solid components in the form of additives.
• the untreated beer comprises total sugars in the range of 0.07g to 0.25 per 100 ml of beer.
• the untreated beer has brix in the range of 3% to 15%, including each value and sub-range within the specified range.
• the treated beer has brix in the range of 0.1% to 5%, including each value and sub-range within the specified range.
• Each possibility represents a separate embodiment of the invention.
• the method comprises providing a system for reducing the sugar content of a beverage, wherein the system comprises: (i) at least one ultrafiltration (UF) unit comprising: a housing defining an inner UF chamber fluidly coupled to a UF inlet port, a UF permeate outlet port, and a UF retentate outlet port; and at least one UF filter disposed within the UF housing wherein the UF filter comprises an ultrafiltration membrane, which has molecular weight cutoff in the range of 5-20 kDa; (ii) at least one nanofiltration (NF) unit comprising: a housing defining an inner NF chamber, wherein the inner NF chamber is fluidly coupled to an NF inlet port, which is fluidly coupled to the UF permeate outlet port, wherein the inner NF chamber is further fluidly coupled to a NF permeate outlet port and to an NF retentate outlet port; and at least one NF filter disposed within the inner NF chamber, wherein the NF filter comprises a nano
• the system further comprises at least one adsorption unit comprising: a housing in the form of an elongated tube column, which is defining an inner adsorption chamber, which contains at least one adsorbent disposed therein, wherein the at least one adsorbent comprises a zeolite, and is active so as to have a higher relative selectivity for disaccharides than for monosaccharides and, optionally, for organic acids; an adsorption unit inlet port fluidly coupled with the NF permeate outlet port; wherein step (d) is performed in the adsorption unit.
• the liquid pump is further configured to: pump the nano-filtered permeate from the inner NF chamber to the inner adsorption chamber through the NF permeate outlet port and the adsorption unit inlet port, and the method further comprises: pumping the ultra-filtered permeate from the inner UF chamber to the inner NF chamber through the UF permeate outlet port and NF inlet port using the pump; and pumping the nano-filtered permeate from the inner NF chamber to the inner adsorption chamber through the NF permeate outlet port and the adsorption unit inlet port using the pump.
• the system further comprises a treated beverage container in fluid communication with the treated beverage outlet port, and the method further comprises pumping the treated beverage from the inner adsorption chamber into the treated beverage container through the treated beverage outlet port using the pump.
• the method comprises pumping the NF permeate from the NF unit as the treated beverage to the treated beverage container.
• the UF retentate outlet port is in fluid communication with the treated beverage container, and wherein the method further comprising pumping the UF retentate to the treated beverage container using the pump.
• the system further comprises at least one centrifugation unit comprising: a housing defining an inner centrifugation chamber, wherein the inner centrifugation chamber is fluidly coupled to a centrifugation inlet port, wherein the inner centrifugation chamber is further fluidly coupled to a centrifuged aqueous medium outlet port and to centrifuged solid outlet port, wherein the centrifuged aqueous medium outlet port is fluidly coupled with the UF inlet port; and a centrifuge disposed within the inner centrifugation chamber; wherein the pump is configured to pump the aqueous medium from the inner centrifugation chamber to the inner UF chamber through the aqueous medium outlet port and the UF inlet port; wherein the method further comprises pumping the aqueous medium from the inner centrifugation chamber to the inner UF chamber through the aqueous medium outlet port and the UF inlet port using the pump.
• the centrifuged solid outlet port is connected to the treated beverage container, and wherein the method further comprising transferring the solids from the inner centrifugation chamber to the treated beverage container, through the solid outlet port.
• the method can comprise controlling valves of all the connections/couplings described herein between various units, chambers, containers, tanks, and/or ports for selectively opening some connection/couplings and closing some connections/couplings simultaneously to use various units, chambers, containers, tanks, and/or ports in different combinations based for example on the requirements associated with the beverage being treated.
• the centrifugation may not be performed and the beverage to be treated can be fed directly into the UF unit.
• the adsorption may not be performed and the NF permeate can be directly fed from the NF unit to the treated beverage container.
• the UF retentate and/or solids from the centrifugation unit may not be fed to the treated beverage container.
• a reduced-sugar beverage prepared according to the method of the present invention.
• a reduced-sugar beverage comprising: beverage organic compounds which are permeable to ultrafiltration and nanofiltration; and is substantially devoid of: beverage organic compounds which are permeable to ultrafiltration but impermeable to nanofiltration, wherein the ultrafiltration is performed through an ultrafiltration membrane, which has molecular weight cutoff in the range of 5-20 kDa and the nanofiltration is performed at a TMP (Trans Membrane Pressure) of at least 10 Bar through a nanofiltration membrane, which has molecular weight cutoff in the range of 150-500 Da.
• TMP Trans Membrane Pressure
• the nanofiltration is performed at a TMP of 10 to 65 Bar.
• the nanofiltration is performed at a TMP of 10 to 20 Bar, 10 to 30 Bar, 10 to 40 Bar, 10 to 50 Bar, 10 to 60 Bar, 10 to 65 Bar, 15 to 25 Bar, 20 to 30 Bar, 25 to 35 Bar, 30 to 40 Bar, 35 to 45 Bar, 40 to 50 Bar, 45 to 55 Bar, 50 to 60 Bar, or 55 to 65 Bar.
• TMP 10 to 20 Bar, 10 to 30 Bar, 10 to 40 Bar, 10 to 50 Bar, 10 to 60 Bar, 10 to 65 Bar, 15 to 25 Bar, 20 to 30 Bar, 25 to 35 Bar, 30 to 40 Bar, 35 to 45 Bar, 40 to 50 Bar, 45 to 55 Bar, 50 to 60 Bar, or 55 to 65 Bar.
• the beverage further comprises beverage compounds which are impermeable to ultrafiltration.
• the reduced-sugar beverage comprises a reduced-sugar juice comprising an isolated citrus juice fraction, and the citrus juice fraction further comprises citrus juice pulp.
• the reduced-sugar beverage comprises the isolated citrus juice fraction and an untreated fruit juice.
• a corresponding untreated citrus juice has an initial Brix/acidity ratio
• the isolated citrus juice fraction has a treated Brix/acidity ratio which is at least 10% lower than the initial Brix/acidity ratio.
• the citrus juice fraction comprises at least 20% less sugar than a corresponding untreated fruit juice.
• the citrus fruit juice is selected from the group consisting of: orange juice, grapefruit juice, clementine juice, mandarine juice and combinations thereof. Each possibility represents a separate embodiment of the invention.
• the reduced- sugar beverage has a ratio of sucrose to total sugars below 70%.
• fraction refers to a composition of matter obtained by performing fractionation in order to separate a specific component or a specific group of components from a mixture containing several different constituents.
• isolated citrus juice fraction refers to a mixture of compounds isolated from a natural fruit juice, as long as the composition is not identical to the natural fruit juice and does not include compounds, which are not present in said natural juice.
• the reduced-sugar beverage comprises a reduced-sugar milk comprising at least 50% less lactose than a corresponding untreated milk. According to some embodiments, the reduced-sugar beverage comprises a reduced-sugar milk comprising at least 80% less lactose than a corresponding untreated milk. According to some embodiments, the treated milk has 50% to 90% less lactose than the untreated milk, including each value and sub-range within the specified range.
• the reduced-sugar beverage comprises a reduced-sugar beer comprising at least 30% less total sugars than a corresponding untreated beer.
• the treated beer has 30% to 80% less total sugars than the untreated beer, including each value and sub-range within the specified range.
• the nanofiltration is conducted with a nanofiltration membrane, which has molecular weight cutoff in the range of 300-500 Da. According to some embodiments, the nanofiltration is conducted with a nanofiltration membrane, which has molecular weight cutoff in the range of 180-500 Da, including each value and sub-range within the specified range.
• the reduced-sugar beverage further comprises an additive selected from the group consisting of: a taste masking agents, a sweetener, a preservative or any combination thereof.
• an additive selected from the group consisting of: a taste masking agents, a sweetener, a preservative or any combination thereof.
• At least one of the ultrafiltration and the nanofiltration is performed through a crossflow filtration unit. According to some embodiments, either or both of the ultrafiltration and nanofiltration is performed using crossflow filtration technique. According to some embodiments, at least the nanofiltration is performed using crossflow filtration technique.
• the reduced-sugar beverage is prepared by the method of the present invention.
• reduced-sugar beverage comprising: beverage organic compounds which are permeable to ultrafiltration and nanofiltration and zeolite adsorption; and is substantially devoid of beverage organic compounds which are permeable to ultrafiltration but impermeable to nanofiltration beverage compounds which are permeable to ultrafiltration and nanofiltration but impermeable to zeolite adsorption, wherein the zeolite has higher relative selectivity for disaccharides than for monosaccharides and, optionally, for organic acids.
• the zeolite is selected from zeolites having a Si/Al molar ratio of at least 10: 1; or wherein the zeolite comprises at least one of Y Zeolite H + and Y Zeolite Ca.
• the reduced-sugar beverage is prepared by the method of the present invention.
• a method for producing an isolated beverage sugar composition from a beverage comprising: (a) providing a beverage; (b) ultra-filtering the aqueous medium through an ultrafiltration membrane, which has molecular weight cutoff in the range of 5-20 kDa to produce an ultra-filtered permeate and an ultra-filtered retentate; (c-i) nano-filtering the ultrafiltered permeate through a nanofiltration membrane, at a TMP (Trans Membrane Pressure) of at least 10 Bar, wherein the nanofiltration membrane has molecular weight cutoff in the range of 150-500 Da to produce a nano-filtered permeate and a nano- filtered retentate, wherein the nano-filtered retentate comprises at least part of the beverage sugar; and (c-ii) isolating and optionally drying the beverage sugar of the nano-filtered retentate to produce an isolated beverage sugar composition comprising the beverage sugar.
• TMP Trans Membrane Pressure
• step (c-ii) comprises drying the beverage sugar of the nano-filtered retentate.
• step (c-i) comprises nano-filtering the ultrafiltered permeate through a nanofiltration membrane, which has molecular weight cutoff in the range of 300-500 Da. According to some embodiments, step (c-i) comprises nano-filtering the ultrafiltered permeate through the nanofiltration membrane, at a TMP of 10 to 65 Bar.
• step (b) and step (c-i) comprises filtering through a crossflow filtration membrane.
• the method further comprises step (d) of contacting at least one adsorbent with the nano-filtered permeate to produce an adsorbed composition and a liquid medium, and filtering the adsorbed composition from liquid medium to form an adsorption filtrate, wherein the at least one adsorbent comprises a zeolite, and wherein the at least one adsorbent has a higher relative selectivity for disaccharides than for monosaccharides and, optionally, for organic acids, thereby producing an isolated beverage sugar composition comprising the beverage sugar.
• the beverage is fruit or vegetable juice
• the beverage sugar composition comprises fruit sugar composition, wherein the fruit sugar composition has Brix in the range of 10 to 70%.
• an isolated beverage sugar composition prepared by the method of the present invention.
• an isolated citrus fruit sugar composition which has Brix in the range of 10% to 50%, pH in the range of 3 to 4, density in the range of 1.01 gr/ml to 1.10 gr/ml, acid content of 0.3% to 1% w/w, sucrose 10% to 50% w/w, glucose 1% to 5% w/w, fructose 1% to 5% w/w and vitamin C 5 mg/100 ml to 50 mg/100 ml.
• the isolated citrus fruit sugar composition has conductivity of 3500 pS to 5000 pS.
• the isolated citrus fruit sugar composition has total sugars 10% to 50% w/w.
• the isolated citrus fruit sugar composition has total amino acid of 0.3% to 1.5% w/w.
• an isolated beverage sugar composition which comprises: beverage organic compounds which are permeable to ultrafiltration but impermeable to nanofiltration; and is substantially devoid of beverage organic compounds which are permeable to nanofiltration wherein the ultrafiltration is performed through an ultrafiltration membrane, which has molecular weight cutoff in the range of 5-20 kDa and the nanofiltration is performed through a nanofiltration membrane, at a TMP (Trans Membrane Pressure) of at least 10 Bar, wherein the nanofiltration membrane has molecular weight cutoff in the range of 150— 500 Da.
• TMP Trans Membrane Pressure
• the nanofiltration is performed at a TMP of 10 to 65 Bar through the nanofiltration membrane.
• At least one of the ultrafiltration and the nanofiltration is performed through a crossflow filtration unit.
• the nanofiltration is conducted with a nanofiltration membrane, which has molecular weight cutoff in the range of 300-500 Da.
• the isolated beverage sugar composition comprises isolated citrus fruit sugar composition, wherein the citrus juice is selected from the group consisting of: orange juice, clementine, mandarin, grapefruit juice and combinations thereof.
• the isolated citrus fruit sugar composition has Brix in the range of 10 to 70%.
• the isolated beverage sugar is prepared by the method of the present invention.
• a method for producing a concentrate of a reduced sugar beverage comprising: (a) providing a beverage; (b) ultra-filtering the beverage through an ultrafiltration membrane, which has molecular weight cutoff in the range of 5-20 kDa to produce an ultra-filtered permeate and an ultra-filtered retentate; (c) nano-filtering the ultra-filtered permeate through a nanofiltration membrane, at a TMP (Trans Membrane Pressure) of at least 10 Bar, wherein the nanofiltration membrane has molecular weight cutoff in the range of 150-500 Da to produce a nano-filtered permeate and a nano-filtered retentate; (d) optionally contacting at least one adsorbent with the nano-filtered permeate to produce an adsorbed composition and a liquid medium, and filtering the adsorbed composition from liquid medium to form an adsorption filtrate, wherein the at least one adsorbent comprises a zeolite, and wherein the at least one a
• the steps (a) to (f) correspond to the steps (a) to (f) of any of the methods described herein and can be performed according to any of the embodiments of the methods described herein.
• the isolated treated beverage can be the NF permeate.
• the isolated treated beverage can be the adsorbent filtrate.
• the isolated treated beverage can be the addition product of step (e).
• the beverage can be any of the beverages described herein, and concentrating the treated beverage into a concentrate thereof provides a more commercially viable product.
• the concentrate can be stored and transported more conveniently than the beverage itself.
• the concentrate of a reduced sugar beverage comprises a concentrate of a reduced sugar fruit or vegetable juice.
• step (g) includes eliminating a certain amount of water content from the treated beverage to achieve the desired concentrate.
• a concentrate of a reduced sugar beverage prepared by the method of any one of the embodiments described herein.
• the concentrate has a treated Brix/acidity ratio which is at least 5% lower than the initial Brix/acidity ratio of a corresponding concentrate of the untreated beverage provided in step (a). According to some embodiments, the concentrate has a treated Brix/acidity ratio which is at least 8% lower than the initial Brix/acidity ratio of a corresponding concentrate of the untreated beverage provided in step (a).
• a corresponding concentrate of the initially provided beverage in step (a) has a brix/acidity ratio of 10 to 17.
• the final concentrate product has a brix/acidity ratio of 10 to 15.
• a concentrate of a reduced sugar fruit or vegetable juice which has Brix of up to 65% a brix/acidity ratio of 10 to 15%, including each value and sub-range within the specified range.
• the Brix and/or brix/acidity ratio of the concentrate of the reduced sugar fruit or vegetable juice depends on the fruit or vegetable juice that it has been prepared from and/or the Brix and/or brix/acidity ratio of the untreated juice initially provided.
• the fruit or vegetable juice is a citrus fruit juice and the citrus fruit juice is selected from the group consisting of orange juice, grapefruit juice and both. Each possibility represents a separate embodiment of the invention.
• Certain embodiments of the present disclosure may include some, all, or none of the above advantages.
• One or more technical advantages may be readily apparent to those skilled in the art from the figures, descriptions and claims included herein.
• specific advantages have been enumerated above, various embodiments may include all, some or none of the enumerated advantages.
• Figure l is a schematic illustration of a system for producing of a reduced sugar content beverage, and an isolated beverage sugar fraction, according to some embodiments.
• Figure 2 is a block diagram representing a process for the preparation of a reduced sugar content beverage, and an isolated beverage sugar fraction, according to some embodiments.
• the present invention provides system and methods for the preparation of reduced-sugar beverage from natural or prepared beverage.
• the methods employ various steps performed at a specific order, which results in a treated beverage, which typically has only up to 1 to 2 gr disaccharide per 100 ml beverage.
• the method of the present invention uses, sequentially, ultrafiltration, nanofiltration and, optionally, zeolite adsorption in order to remove excess sugars.
• the method includes reconstitution of the ultrafiltration retentate to the sugar-reduced beverage, according to some embodiments.
• the present invention provides a sugar extract produced upon isolating and optionally drying the (previously ultra-filtered) nanofiltration retentate, which is described herein.
• the sugar-reducing method of the invention removes naturally-occurring sugar and produces low sugar beverages, while aiming at maintaining the natural origin of the beverage and its sensory and nutritional characteristics.
• the present method removes sugars from a complex mixtures in a substantially selective manner, without mixing any non-natural chemical substance to it and without significantly changing its chemical composition, other than removing sugar and, optionally, organic acids.
• the present method is such that it allows for reducing the sugar content in the beverage typically by 30% or more without significantly impacting the beverage sensory and nutritional value beyond sugar reduction.
• the beverage can be a fruit or vegetable juice, milk, beer, or other beverage comprising complex sugars, specifically including disaccharides and monosaccharides.
• the embodiments of the presently disclosed subject matter relate to selectively removing the disaccharides while maintaining the sensory and nutritional characteristics of the beverage.
• the beverage being treated is a faiit juice or a vegetable juice
• the product isolated juice maintains at least 80% of the original vitamin C content.
• the beverage can contain sugars including only monosaccharides and no disaccharides.
• Some examples of such beverages include apple juice and grape juice.
• presently disclosed subject matter relate to selectively removing at least a part of sugars while maintaining the sensory and nutritional characteristics of the beverage.
• the present invention provides a system for producing the reduced- sugar beverage and beverage sugar fraction of the present invention.
• the sugar fraction extracted from the beverage has been generally referred to herein as beverage sugar.
• the system includes, according to some embodiments, an ultrafiltration unit, a nanofiltration unit and, optionally, an adsorption unit, according to some embodiments.
• Figure 1 schematically illustrates a system 100, which is elaborated herein and is configured to receive an untreated beverage and produce a reduced-sugar beverage, generally referred to herein as treated beverage or isolated treated beverage as well, therefrom.
• the system 100 is configured to reduce the sugar content of a fruit or vegetable juice, milk, beer, or other beverages including sugar content comprising disaccharides and monosaccharides.
• the system 100 is configured to simultaneously produce reduced-sugar beverage and an isolated beverage sugar composition from a natural or prepared beverage.
• the system 100 of Figure 1 comprises four main modules, each of which is configured to separate or isolate different constituents of the liquid composition it receives, according to some embodiments. It is to be understood that the composition received in each module may be the original untreated beverage (e.g., for the first module) or any of the intermediate beverage compositions treated in previous modules and entering the next module.
• the main modules or assemblies of the present system 100 comprise: a centrifugation unit 110, an ultrafiltration (UF) unit 120, a nanofiltration (NF) unit 130 and an adsorption unit 140.
• the terms “module”, “assembly” and “unit” are used herein interchangeably. It is to be understood herein that not necessarily all the four modules 110, 120, 130, and 140 are used for treating all the beverages, and these modules can be selectively used (or selectively bypassed) based for example on the beverage being treated and/or requirements of the resulting treated beverage. For instance, in some embodiments, the centrifugation unit 110 and/or the adsorption unit 140 may not be used, and accordingly are to be understood as being optional.
• the system 100 has been described herein as including all these modules for the sake of clarity of the description. Additional units in system 100 include a treated beverage container 150 and isolated sugar composition container 160, and are dependent on the use of the system 100, as elaborated below.
• the system 100 includes a centrifugation unit 110 as schematically shown in Figure 1.
• the function of the centrifugation unit 110 is to receive natural untreated beverage and to separate the undissolved solids (e.g., the juice pulp if the beverage is a fruit or vegetable juice) from the liquid aqueous beverage.
• centrifugation unit 110 comprises a centrifugation unit housing 112, which defines an inner centrifugation chamber 114.
• the inner centrifugation chamber 114 is fluidly coupled to a centrifugation inlet port 116.
• the untreated beverage which is the starting material or composition of the present process, is inserted to the system 100 through the centrifugation inlet port 116.
• the centrifugation inlet port 116 is connected to a beverage inlet port 105 through which the beverage is inserted to the system 100.
• the beverage inlet port 105 may be, for example a funnel through which the beverage is conveniently inserted or is a liquid pipe connected to a beverage source. Each possibility represents a separate embodiment of the invention.
• the beverage inlet port 105 is a funnel.
• the beverage inlet port 105 comprises a pipe connected to a beverage source.
• the beverage inlet port 105 comprises a pipe connected to a beverage source.
• the system 100 further comprises a juice extractor (e.g., a juicer; not shown in Figure 1), which is configured to squeeze juice from fruits or vegetables and transfer the squeezed juice to the system 100 through the juice inlet port 105.
• a juice extractor e.g., a juicer; not shown in Figure 1
• the centrifugation unit 110 in addition to the centrifugation inlet port 116, the centrifugation unit 110 has two outlet ports, the centrifuged aqueous medium outlet port 118, for the centrifuged aqueous medium and the centrifuged solid outlet port 119, for the separated solids.
• the centrifugation unit 110 comprises a centrifuge 115 disposed within the inner centrifugation chamber 114.
• the term “centrifuge” as used herein refers to a device that uses centrifugal force to separate various components of a fluid. This is achieved by spinning the fluid at high speed within a container, thereby separating fluids of different densities or liquids from solids. It works by causing denser substances and particles to move outward in the radial direction. At the same time, objects that are less dense are displaced and move to the center.
• the centrifuge 115 is configured to separate solid components of a beverage from its liquid components. According to some embodiments, the centrifuge 115 is configured to operate at a rotational rate of 20 to 200 RPM. According to some embodiments, the centrifuge 115 is configured to operate at least at a rotational rate of about 50 RPM.
• the term “about” refers to a range of values ⁇ 20%, or ⁇ 10% of a specified value.
• the phrase “the percentage is about 5% w/w “ includes ⁇ 20% of 5, or from 4% to 6%, or from 4.5% to 5.5%.
• “about 50 RPM” refers to ⁇ 20% of 50 RPM, or from 40 to 60 RPM, or from 45 to 55 RPM.
• the inner centrifugation chamber 114 fluidly coupled to a centrifuged aqueous medium outlet port 118.
• the centrifuged aqueous medium outlet port 118 is fluidly coupled with the UF inlet port 126, which is described herein.
• the term “fluidly coupled” means that two or more components are connected to one another such that a gas or liquid or liquid containing solids may be conveyed between them.
• any of the recitations of the term “fluidly coupled” refers to an arrangement, wherein liquid or gas or any flowy mixture of solid, liquid, and/or gas may be conveyed between different components of the system 100.
• any of the recitations of the term “fluidly coupled” refers to an arrangement, wherein dry or wet solids may be conveyed therethrough.
• the centrifuged liquid outlet port 118 is connected to the UF inlet port 126 through a centrifuge-UF pipe 1112.
• the centrifuge- UF pipe 1112 may be flexible or rigid, as long as it may convey liquids, such as beverage therein.
• the centrifuge-UF pipe 1112 comprises a centrifuge- UF flow valve 212, configured to regulate liquid flow from the centrifugation unit 110 to the UF unit 120.
• the centrifuge-UF flow valve 212 is a unidirectional valve, which is configured to regulate liquid flow in the direction from the centrifugation unit 110 to the UF unit 120.
• the inner centrifugation chamber 114 fluidly coupled to a centrifuged solid outlet port 119.
• the centrifuged solid outlet port 119 is connected with the treated beverage container 150, which is described herein.
• the centrifuged solid outlet port 119 is the port, though with the separated solids (e.g., the pulp if the beverage is a fruit or vegetable juice) exits the centrifugation unit 110.
• the centrifuged aqueous medium outlet port 118 and the centrifuged solid outlet port 119 is the same port, used alternately or selectively for solids and for liquids.
• the centrifuged solid outlet port 119 is coupled to the treated beverage container 150 through a centrifuge-treated beverage container pipe 1115.
• the centrifuge-treated beverage container pipe 1115 may be flexible or rigid, as long as it may convey dry or wet solids. Each possibility represents a separate embodiment of the invention.
• the centrifuge-treated beverage container pipe 1115 comprises a centrifuge-treated beverage container flow valve 251, configured to regulate solid or liquid flow from the centrifugation unit 110 to the treated beverage container 150.
• the centrifuge-treated beverage container flow valve 251 is a unidirectional valve, which is configured to regulate liquid flow in the direction from the centrifugation unit 110 to the treated beverage container 150.
• the system 100 further comprises at least one pump (not shown).
• the pump(s) is connected to any one or more of the units of the system 100 (e.g., to the centrifugation unit 110, the UF unit 120, the NF unit 130, and/or the adsorption unit 140; each possibility represents a separate embodiment of the invention), and configured to mechanically displace liquid or solid components between the different components of the system 100.
• the pump is configured to pump liquids from the inner centrifugation chamber 114 to the inner UF chamber 124 through the aqueous medium outlet port 118 and the UF inlet port 126.
• the beverage inlet port 105 can be fluidly coupled directly to the UF inlet port 126 via a centrifuge bypass line CBL being regulated by a centrifuge bypass valve CBV.
• the centrifugation unit 110 may not be used, especially when the beverage does not have solid components and/or because the solid components are filtered by the ultrafiltration unit 120.
• the centrifuge bypass valve CBV can be opened and the beverage can be fed directly to the UF inlet port 126 without feeding the same to the centrifugation inlet port 116, and accordingly, the centrifuge-UF flow valve 212 and the centrifuge-treated beverage container flow valve 251 can be closed.
• the centrifuge bypass valve CBV is a unidirectional valve, which is configured to regulate liquid flow in the direction from the beverage inlet port 105 to the UF unit 120.
• the pump is configured to pump liquids from the beverage inlet port 105 to UF unit 120 through the centrifuge bypass line CBL and the UF inlet port 126.
• a part of the untreated beverage can be fed into the UF unit 120 after processing in the centrifugation unit 110 while a part of the untreated beverage can be fed directly via the centrifuge bypass line CBL to the UF unit 120.
• the UF unit 120 comprises a UF unit housing 122, which defines an inner UF chamber 124.
• the inner UF chamber 124 is fluidly coupled to the UF inlet port 126.
• the aqueous medium separated from the solids in the centrifugation unit 110 or the untreated beverage from the beverage inlet port 105 is inserted to the UF unit 120 through the UF inlet port 126.
• the UF unit 120 in addition to the UF inlet port 126, the UF unit 120 has two outlet ports, a UF permeate outlet port 128, for the UF permeate, and a UF retentate outlet port 129, for the separated UF retentate.
• the UF unit 120 comprises a UF filter 125 disposed within the inner UF chamber 124.
• the terms “UF filter” and “ultrafilter” are interchangeable and refer to any filter capable of separating components of a solution or mixture on the basis of molecular size and/or shape, and has a filter membrane with pore size of about 0.01 to about 0.1 microns, or micrometers, including each value and sub-range within the specified range.
• an ultrafilter may operate such that under an applied pressure difference across an ultrafiltration membrane, solvent and small solute species pass through the membrane and are collected as permeate while larger solute species are retained by the membrane and recovered as a concentrated retentate.
• the UF filter 125 is configured to separate solid components of a beverage from its liquid components. According to some embodiments, the UF filter 125 is configured to retain at least a portion of vitamin C contained in beverages, specifically for example in case the beverage is a fruit or vegetable juice, such as orange juice. According to some embodiments, the UF filter 125 is configured to retain at least 0.1%, at least 0.5%, at least 1%, at least 5%, at least 10%, at least 20%, at least 30%, at least 40%, or at least 50%, of vitamin C contained in fruit juices. Each possibility represents a separate embodiment of the invention.
• the UF filter 125 has molecular weight cutoff in the range of 5-100 kilodalton (kDa). According to some embodiments, the UF filter 125 has molecular weight cutoff in the range of 5-99 kDa. According to some embodiments, the UF filter 125 has molecular weight cutoff in the range of 5-90 kDa. According to some embodiments, the UF filter 125 has molecular weight cutoff in the range of 5-75 kDa. According to some embodiments, the UF filter 125 has molecular weight cutoff in the range of 5-50 kDa. According to some embodiments, the UF filter 125 has molecular weight cutoff in the range of 5-25 kDa.
• the UF filter 125 has molecular weight cutoff in the range of 5-20 kDa. According to some embodiments, the UF filter 125 has molecular weight cutoff in the range of 5-15 kDa. According to some embodiments, the UF filter 125 has molecular weight cutoff in the range of 5-10 kDa.
• the UF filter 125 is configured to operate at a pressure of about 2 to about 8 Bar, including each value and sub-range within the specified range.
• the pump is configured to operate at a pressure of 40 to 100 PSI, 45 to 95 PSI, 50 to 90 PSI, 55 to 85 PSI, 60 to 80 PSI or 65 to 75 PSI.
• the UF filter 125 is configured to operate at a pressure of 40 to 100 PSI, 45 to 95 PSI, 50 to 90 PSI, 55 to 85 PSI, 60 to 80 PSI or 65 to 75 PSI.
• Each possibility represents a separate embodiment of the invention.
• the pressure at the retentate side of the UF filter 125 is in the range of 35 to 95 PSI, 40 to 90 PSI, 45 to 85 PSI, 50 to 80 PSI, 55 to 75 PSI or 60 to 70 PSI.
• Each possibility represents a separate embodiment of the invention.
• the system 100 is configured to operate, such that the UF retentate volume flow rate between the pump and the UF filter 125 is in the range of 6 to 12, 7 to 11, 8 to 10 or 8.5 to 9.5 liters per minute. Each possibility represents a separate embodiment of the invention. According to some embodiments, the system 100 is configured to operate, such that the UF permeate volume flow rate at the side of UF filter 125, which is distal from the pump, is in the range of 1 to 2, 1.25 to 1.75 or 1.4 to 1.6 liters per minute. Each possibility represents a separate embodiment of the invention.
• the UF unit 120 is a crossflow filtration unit and the ultrafiltration is performed by crossflow filtration technique.
• the beverage can be filtered through the UF membrane (also referred to herein as UF filter) in multiple filtration cycles while flowing tangentially along one or more UF membranes using the crossflow filtration technique.
• the pump is driven by a Variable Frequency Drive (VFD).
• VFD Variable Frequency Drive
• the pump is operated by a VFD of about 35Hz.
• the inner UF chamber 124 is fluidly coupled to a UF permeate outlet port 128.
• the UF permeate outlet port 128 is fluidly coupled with the NF inlet port 136, which is described herein.
• the UF permeate outlet port 128 is connected to the NF inlet port 136 through a UF-NF pipe 1213.
• the UF-NF pipe 1213 may be flexible or rigid, as long as it may convey liquids, such as the beverage therein. Each possibility represents a separate embodiment of the invention.
• the UF-NF pipe 1213 comprises a UF-NF flow valve 213, configured to regulate liquid flow from the UF unit 120 to the NF unit 130.
• the UF-NF pipe 1213 is a unidirectional valve, which is configured to regulate liquid flow in the direction from the UF unit 120 to the NF unit 130.
• the inner UF chamber 124 is fluidly coupled to the UF retentate outlet port 129.
• the UF retentate outlet port 129 is fluidly coupled with the treated beverage container 150, which is described herein.
• the UF retentate outlet port 129 is the port, through with the separated UF retentate exits the UF unit 120.
• the UF permeate outlet port 128 and the UF retentate outlet port 129 is the same port, used alternately or selectively for solids and for liquids.
• the UF retentate outlet port 129 is coupled to the treated beverage container 150 through a UF-treated beverage container pipe 1215.
• the UF- treated beverage container pipe 1215 may be flexible or rigid, as long as it may convey liquids and/or solids. Each possibility represents a separate embodiment of the invention.
• the UF- treated beverage container pipe 1215 comprises a UF- treated beverage container flow valve 215, configured to regulate solid or liquid flow from the UF unit 120 to the treated beverage container 150.
• the UF- treated beverage container flow valve 215 is a unidirectional valve, which is configured to regulate liquid flow in the direction from the UF unit 120 to the treated beverage container 150.
• the pump is configured to pump liquid and/or solid materials from the inner UF chamber 124 to the inner NF chamber 134 through the UF permeate outlet port 128 and the NF inlet port 136. According to some embodiments, the pump is configured to pump liquid and/or solid materials from the inner UF chamber 124 to the treated beverage container 150 through the UF retentate outlet port 129.
• the NF unit 130 comprises aNF unit housing 132, which defines an inner NF chamber 134.
• the inner NF chamber 134 is fluidly coupled to the NF inlet port 136.
• the UF permeate separated from the corresponding retentate in the UF unit 120 is inserted to the NF unit 130 through the NF inlet port 136.
• the NF inlet port 136 is connected to the UF unit 120 through the UF-NF pipe 1213.
• the UF-NF pipe 1213 and the UF- NF flow valve 213 are elaborated above.
• the NF unit 130 in addition to the NF inlet port 136, the NF unit 130 has two outlet ports, a NF permeate outlet port 138, for the NF permeate, and a NF retentate outlet port 139, for the separated NF retentate.
• the NF unit 130 comprises a NF filter 135 disposed within the inner NF chamber 134.
• NF filter and “nanofilter” are interchangeable and refer to any filter capable of separating components of a solution or mixture on the basis of molecular size and/or shape, and has a filter membrane with pore size of about 0.5 to about 10 nanometers, including each value and sub-range within the specified range.
• a nanofilter may operate such that under an applied pressure difference across a nanofiltration membrane, solvent and small solute species pass through the membrane and are collected as permeate while larger solute species are retained by the membrane and recovered as a concentrated retentate.
• the NF filter 135 has molecular weight cutoff in the range of 150 to 500 Dalton (Da), including each value and sub-range within the specified range. According to some embodiments, the NF filter 135 has molecular weight cutoff in the range of 180 to 500 Dalton (Da). According to some embodiments, the NF filter 135 has molecular weight cutoff in the range of 200 to 500 Dalton (Da). According to some embodiments, the NF filter 135 has molecular weight cutoff in the range of 225 to 500 Dalton. According to some embodiments, the NF filter 135 has molecular weight cutoff in the range of 250 to 500 Dalton. According to some embodiments, the NF filter 135 has molecular weight cutoff in the range of 275 to 500 Dalton. According to some embodiments, the NF filter 135 has molecular weight cutoff in the range of 300 to 500 Dalton.
• the NF filter 135 is configured to operate at a pressure of about 2 to about 8 Bar, including each value and sub-range within the specified range.
• the pump is configured to operate at a pressure of 75 to 400 PSI, 100 to 350 PSI, 125 to 350 PSI, 150 to 300 PSI, 175 to 275 PSI or 200 to 250 PSI.
• the NF filter 135 is configured to operate at a pressure of 75 to 400 PSI, 100 to 350 PSI, 125 to 350 PSI, 150 to 300 PSI, 175 to 275 PSI or 200 to 250 PSI.
• Each possibility represents a separate embodiment of the invention.
• the pressure at the retentate side of the NF filter 135 is in the range of 75 to 400 PSI, 100 to 350 PSI, 125 to 350 PSI, 150 to 300 PSI, 175 to 275 PSI or 200 to 250 PSI.
• the system 100 is configured to operate, such that the NF retentate volume flow rate between the pump and the NF filter 135 is in the range of 6 to 12, 7 to 11, 8 to 10 or 8.5 to 9.5 liters per minute.
• Each possibility represents a separate embodiment of the invention.
• the system 100 is configured to operate, such that the NF permeate volume flow rate at the side of NF filter 125, which is distal from the pump, is in the range of 2.25 to 3.78, 2.5 to 3.5 or 2.75 to 3.25 liters per minute.
• the NF permeate volume flow rate at the side of NF filter 125 which is distal from the pump, is in the range of 2.25 to 3.78, 2.5 to 3.5 or 2.75 to 3.25 liters per minute.
• the NF unit 130 is a crossflow filtration unit and the nanofiltration is performed by crossflow filtration technique.
• the beverage can be filtered through the NF membrane (also referred to herein as NF filter) in multiple filtration cycles while flowing tangentially along one or more NF membranes using the crossflow filtration technique.
• NF membrane also referred to herein as NF filter
• the pump is driven by a Variable Frequency Drive (VFD).
• VFD Variable Frequency Drive
• the pump is operated by a VFD of about 35Hz.
• the pump is configured to facilitate the nanofiltration of the ultra-filtered permeate through the NF filter, at a TMP (Trans Membrane Pressure) of at least 10 Bar. According to some embodiments, the pump is configured to facilitate the nanofiltration of the ultra-filtered permeate through the NF filter, at a TMP of 10 to 65 Bar, including each value and sub-range within the specified range.
• TMP Trans Membrane Pressure
• the pump is configured to facilitate the nanofiltering of the ultra-filtered permeate through the at least one NF filter, at a TMP of 10 to 20 Bar, 10 to 30 Bar, 10 to 40 Bar, 10 to 50 Bar, 10 to 60 Bar, 10 to 65 Bar, 15 to 25 Bar, 20 to 30 Bar, 25 to 35 Bar, 30 to 40 Bar, 35 to 45 Bar, 40 to 50 Bar, 45 to 55 Bar, 50 to 60 Bar, or 55 to 65 Bar.
• TMP 10 to 20 Bar, 10 to 30 Bar, 10 to 40 Bar, 10 to 50 Bar, 10 to 60 Bar, 10 to 65 Bar, 15 to 25 Bar, 20 to 30 Bar, 25 to 35 Bar, 30 to 40 Bar, 35 to 45 Bar, 40 to 50 Bar, 45 to 55 Bar, 50 to 60 Bar, or 55 to 65 Bar.
• the system further comprises a controller (not shown) for increasing the TMP during at least a part of the nanofiltration.
• the controller for increasing the TMP during a part of or whole of the nanofiltration either continuously or in discrete (periodic or aperiodic) steps time to time.
• the controller can be the same controller that controls all the operations of the system.
• the controller can be a specific controller for controlling the TMP.
• the controller controls or regulates (for example, increases) the TMP by controlling the liquid pump.
• the controller controls or regulates (for example, increases) the TMP by controlling the opening / closing and/or open/close extent of a valve or by controlling other components effecting the TMP.
• the controller increases the TMP continuously.
• the controller increases the TMP periodically or in discrete steps.
• the controller can be a preprogrammed controller to automatically regulate the TMP according to a predetermined pattern.
• the inner NF chamber 134 is fluidly coupled to a NF permeate outlet port 138.
• the NF permeate outlet port 138 is fluidly coupled with the adsorption inlet port 146, which is described herein.
• the NF permeate outlet port 138 is connected to the adsorption inlet port 146 through aNF-adsorption pipe 1314.
• the NF-adsorption pipe 1314 may be flexible or rigid, as long as it may convey liquids, such as the beverage therein. Each possibility represents a separate embodiment of the invention.
• the NF-adsorption pipe 1314 comprises a NF- adsorption flow valve 314, configured to regulate liquid flow exiting the NF unit 130.
• the NF-adsorption flow valve 314 is a unidirectional valve, which is configured to regulate liquid flow in the direction from the NF unit 130 to the adsorption unit 140 or the treated beverage container 150.
• the inner NF chamber 134 is fluidly coupled to the NF retentate outlet port 139.
• the NF retentate outlet port 139 is fluidly coupled with the isolated sugar composition container 160, which is described herein. As detailed above, the NF retentate outlet port 139 is the port, though with the separated NF retentate exits the NF unit 130.
• the isolated sugar composition container 160 is configured to contain the sugar fraction, which is the NF retentate, and may be used in the industry. According to some embodiments, the isolated sugar composition may be further dried. Suitable drying devices include a blower for air/gas flow drying, a heater for promoting evaporation or a vacuum device. Each possibility represents a separate embodiment of the invention. According to some embodiments, the NF retentate outlet port 139 is coupled to the isolated sugar composition container 160 through a NF-sugar container pipe 1316.
• the NF-sugar container pipe 1316 may be flexible or rigid, as long as it may convey liquids and/or solids. Each possibility represents a separate embodiment of the invention.
• the NF-sugar container pipe 1316 comprises NF-sugar container flow valve 316, configured to regulate solid or liquid flow from the NF unit 130 to the isolated sugar composition container 160.
• the NF-sugar container flow valve 316 is a unidirectional valve, which is configured to regulate flow in the direction from the NF unit 130 to the isolated sugar composition container 160.
• the pump is configured to pump liquid and/or solid materials from the inner NF chamber 134 to the inner adsorption chamber 144 through the NF permeate outlet port 138 and the adsorption inlet port 146. According to some embodiments, the pump is configured to pump liquid and/or solid materials from the inner NF chamber 134 to the isolated sugar composition container 160 through the NF retentate outlet port 139.
• the adsorption unit 140 comprises an adsorption unit housing 142, which defines an inner adsorption chamber 144.
• the inner adsorption chamber 144 is fluidly coupled to the adsorption inlet port 146.
• the adsorption unit housing 142 in the form of an elongated tube column.
• the NF permeate separated from the corresponding retentate in the NF unit 130 is inserted to the adsorption unit 130 through the adsorption inlet port 146, which is regulated by an adsorption inlet valve 147, described herein further below.
• the adsorption inlet port 146 is connected to the NF unit 130 through the NF-adsorption pipe 1314.
• the NF-adsorption pipe 1314 and the NF-adsorption flow valve 314 are elaborated above.
• the adsorption unit 140 in addition to the adsorption inlet port 146, the adsorption unit 140 has an adsorption outlet port 148 for the liquid not adsorbed within the inner adsorption chamber 144. According to some embodiments, the adsorption unit 140 comprises at least one adsorbent 145 disposed within the inner adsorption chamber 144.
• the at least one adsorbent 145 comprises a zeolite. According to some embodiments, the at least one adsorbent 145 is active so as to have a higher relative selectivity for disaccharides than for monosaccharides. According to some embodiments, the at least one adsorbent 145 is active so as to have a higher relative selectivity for disaccharides than for organic acids.
• the at least one adsorbent 145 is selected from zeolites having a Si/Al molar ratio of at least 10: 1. According to some embodiments, the at least one adsorbent 145 comprises at least one of Y Zeolite H + and Y Zeolite Ca. According to some embodiments, the at least one adsorbent 145 adsorbent is associated with a carrier selected from beads, granules, fibers, tubes, high-porosity scaffold, and combinations thereof. Each possibility represents a separate embodiment of the invention. According to some embodiments, the carrier comprises beads. According to some embodiments, the beads are of approximately 0.1 millimeter to approximately 15 millimeters in diameter.
• the at least one adsorbent 145 is a powder embedded into the beads.
• the beads comprise a food grade material comprising at least one of hydrogels, organic resins, glass, polymers, carbons, and ceramics.
• the beads are made of a porous material.
• the beads or granules comprise pores of approximately 0.1 micrometers (pm) to approximately 100 pm in diameter.
• the granules are approximately 1 mm to approximately 15 mm in diameter.
• the beads comprise a non-porous material coated with zeolite powder.
• the carrier comprises at least one of fibers and tubes.
• the surface of the fibers and the tubes is coated with a zeolite powder.
• the adsorption unit 140 is configured to operate at a pressure of about 1 to about 10 Bar, including each value and sub-range within the specified range.
• the inner adsorption chamber 144 is fluidly coupled to the adsorption outlet port 148.
• the adsorption outlet port 148 is fluidly coupled with the treated beverage container 150, which is described herein.
• the adsorption outlet port 148 is connected to the treated beverage container 150 through an adsorption-treated beverage pipe 1415 and a treated beverage outlet port 149.
• the adsorption-treated beverage pipe 1415 may be flexible or rigid, as long as it may convey liquids, such as the beverage therein. Each possibility represents a separate embodiment of the invention.
• the adsorption-treated beverage pipe 1415 comprises an adsorption- treated beverage flow valve 415 between the adsorption outlet port 148 and treated beverage outlet port 149, configured to regulate liquid flow from the adsorption unit 140 to the treated beverage outlet port 149 and thereby to the treated beverage container 150.
• the adsorption-treated beverage flow valve 415 is a unidirectional valve, which is configured to regulate liquid flow in the direction from the adsorption unit 140 to the treated beverage outlet port 149.
• the pump is configured to pump liquid and/or solid materials from the inner adsorption chamber 144 to the treated beverage container 150 through the adsorption outlet port 148 and the treated beverage outlet port 149.
• the adsorption unit 140 is bypassed or is not used, and the NF permeate outlet port 138 is fluidly coupled directly to the treated beverage outlet port 149 via an adsorption bypass line ABL being regulated by an adsorption bypass valve ABV.
• the adsorption bypass valve ABV can be opened and the NF permeate can be fed as treated beverage directly to the treated beverage container 150 via the treated beverage outlet port 149, without feeding the NF permeate to the adsorption unit 140.
• the adsorption bypass line is connected to the NF-adsorption pipe 1314 upstream of the adsorption inlet valve 147.
• the system 100 can comprise a separate fluid connection between the NF permeate outlet port 138 and the treated beverage outlet port 149 (or directly to the treated beverage container 150), exclusive of the NF- adsorption pipe 1314.
• the adsorption inlet valve 147 and the adsorption-treated beverage flow valve 415 can be closed, and the adsorption bypass valve ABV can be opened.
• the adsorption bypass valve ABV is a unidirectional valve, which is configured to regulate liquid flow in the direction from the NF permeate outlet port 138 to the treated beverage outlet port 149 or the treated beverage container 150.
• the pump is configured to pump liquids from the NF permeate outlet port 138 to the treated beverage outlet port 149 or the treated beverage container 150 through the adsorption bypass line ABL.
• a part of the NF permeate can be fed into the treated beverage container 150 after processing in the adsorption unit 140 while a part of the NF permeate can be fed directly via the adsorption bypass line ABL to the treated beverage container 150.
• the treated beverage container 150 is configured to contain liquids and solids, such as the treated beverage exiting the NF unit 130 and/or the adsorption unit 140, and optionally, the solids exiting the centrifugation unit 110 and/or the UF retentate exiting the UF unit 120.
• the treated beverage container 150 comprises a mixing device configured to mix the contents received therewithin.
• FIG. 2 is a block diagram representing a method for the preparation of a reduced sugar content beverage, and an isolated beverage sugar fraction, according to some embodiments.
• the method for reducing the sugar content of a beverage comprises the following main steps: (a) providing a beverage; (b) ultrafiltering the beverage to produce an ultra-filtered permeate and an ultra-filtered retentate; (c) nano-filtering the ultra-filtered permeate to produce a nano-filtered permeate and a nano-filtered retentate; (d) optionally contacting at least one adsorbent with the nano-filtered permeate to produce an adsorbed composition and a liquid medium, and filtering the adsorbed composition from liquid medium to form an adsorption filtrate, wherein the at least one adsorbent comprises a zeolite, and wherein the at least one adsorbent has a higher relative selectivity for disaccharides than for monosaccharides and, optionally, for organic acids; e) optionally adding at least one additive to the nano-filtered permeate or to the adsorption filtrate; and (f) isolating the nano-filtered permeate of
• the present method is used for reducing the sugar content of a beverage, which is either fruit or vegetable juice, milk, beer, or any other beverage, which includes sugar.
• the method comprises the following main steps: (a) providing a beverage; (b) ultra-filtering the beverage to produce an ultrafiltered permeate and an ultra-filtered retentate; (c) nano-filtering the ultra-filtered permeate to produce a nano-filtered permeate and a nano-filtered retentate; (d) optionally contacting at least one adsorbent with the nano-filtered permeate to produce an adsorbed composition and a liquid medium, and filtering the adsorbed composition from liquid medium to form an adsorption filtrate, wherein the at least one adsorbent comprises a zeolite, and wherein the at least one adsorbent has a higher relative selectivity for disaccharides than for monosaccharides and, optionally, for organic acids; (e) optionally adding at least one additive to the nano-filtered per
• the method for producing an isolated beverage sugar composition from a beverage comprises the following main steps: (a) providing a beverage; (b) ultra-filtering the aqueous medium to produce an ultrafiltered permeate and an ultra-filtered retentate; (c-i) nano-filtering the ultra-filtered permeate to produce a nano-filtered permeate and a nano-filtered retentate, wherein the nano-filtered retentate comprises at least part of the fruit or vegetable sugar; and (c-ii) isolating and optionally drying the sugar of the nano-filtered retentate to produce an isolated beverage sugar composition comprising the beverage sugar.
• reduced-sugar “reduced-sugar content” and “reduced-sugar concentration”, which are used when referring to the present method of reducing the sugar content of a beverage, are interchangeable and refer, according to some embodiments, to a method, which receives a starting composition having a first concentration/content of sugars and produces an end composition having a second concentration/content of sugars, which is lower than the first concentration/content.
• reduced-sugar “reduced-sugar content” refer to the end product produced by such method.
• the method begins in block 1000, according to some embodiments, of providing an untreated beverage, which can be a fruit or vegetable juice, milk, beer, or any other beverage containing sugar content including disaccharides and optionally monosaccharides. It is to be understood that the specified exemplary embodiments of Figure 2 may be applied to other sugar-containing beverages, which may be depleted of sugars through the present method, according to some embodiments.
• Block 1000 relates to step (a) of providing a beverage.
• the beverage comprises insoluble solids dispersed in an aqueous medium.
• juices when squeezed from the fruit consist mostly of an aqueous medium mixed with insoluble fruit pulp.
• pulp refers to that portion of a fruit or vegetable which remains after removal of the juice from the fruit/vegetable and typically includes various ratios of cellulose, hemicellulose, lignin, pectic material, and other water insoluble materials.
• the insoluble solids comprise fruit juice pulp.
• step (a) comprises providing a fruit juice, which comprises fruit juice pulp dispersed in an aqueous juice medium.
• the fruit juice is selected from the group consisting of citrus fruits, apple juice, apricot juice, banana juice, blackberry juice, blueberry juice, cherry juice, cranberry juice, grape juice, guava juice, mango juice, passion fruit juice, papayajuice, peach juice, pineapple juice, coconutjuice, plum juice, pear juice, pomegranates, raspberry juice and mixtures thereof.
• the fruit juice is a citrus juice.
• the citrus juice is selected from the group consisting of: orange juice, grapefruit juice, citron juice, clementine juice, lemonade, tangerine juice and mixtures thereof.
• the fruit juice is orange juice, grapefruit juice or a mixture thereof.
• the fruit juice is orange juice.
• the fruit juice is grapefruit juice.
• the fruit juice is apple juice.
• the vegetable juice is selected from the group consisting of: carrot juice and beet juice.
• the untreated juice has an initial Brix/acidity ratio of 12.5 to 18.5.
• the empirical Brix/acid ratio found by dividing the acid-corrected and temperature-corrected Brix by the % titratable acidity w/w as citric acid (B/A ratio), is one of the most commonly used indicators of juice quality as well as fruit or vegetable maturity.
• the natural juice provided in step (a) (block 1000) has Brix of 7 to 15%, 9% to 13% or 10% to 12%.
• each possibility represents a separate embodiment of the invention and including each value and sub-range within the specified range.
• step (a) further comprises providing a fruit or vegetable and squeezing the fruit or vegetable to produce the untreated fruit or vegetable juice.
• the squeezing is performed by a juice extractor (e.g., a juicer).
• the squeezing is performed by a juice extractor), which is configured to squeeze juice from fruits or vegetables, and step (a) further comprises transferring the squeezed juice to the system 100 through the juice inlet port 105.
• step (a) comprises providing milk, which comprises naturally existing sugars including disaccharides such as lactose.
• the milk which is to treated by the present method may include solid components in the form of additives.
• the milk contains calcium, protein, along with other minerals and vitamins.
• the untreated milk comprises 4.7 g lactose per 100 g of milk.
• the untreated milk has brix in the range of 5% to 15%, including each value and sub-range within the specified range. Each possibility represents a separate embodiment of the invention.
• the treated milk has brix in the range of 4% to 8%, including each value and sub-range within the specified range. Each possibility represents a separate embodiment of the invention.
• step (a) comprises providing beer, which comprises naturally existing sugars including disaccharides such as maltose and monosaccharides such as glucose.
• the beer which is to treated by the present method may include solid components in the form of additives.
• the untreated beer comprises total sugars in the range of 0.07g to 0.25 per 100 ml of beer.
• the untreated beer has brix in the range of 3% to 15%, including each value and sub-range within the specified range.
• the treated beer has brix in the range of 0.1% to 5%, including each value and sub-range within the specified range.
• Each possibility represents a separate embodiment of the invention.
• Block 1010 shown in Figure 2 relates to an optional step of separating solids from the aqueous medium of the beverage.
• the method comprises separating at least part of the solids from the aqueous medium after step (a).
• the method comprises separating at least part of the pulp from the aqueous medium.
• the method comprises separating at least 10-80% of the pulp from the aqueous medium.
• separating at least part of the solids from the aqueous medium includes one or more of centrifugation and filtration.
• the step of separating solids from the aqueous medium of the beverage does not include ultrafiltration.
• the step of separating solids from the aqueous medium of the beverage does not include nanofiltration.
• the step of separating solids from the aqueous medium of the beverage does not include any one of ultrafiltration and nanofiltration.
• the step of block 1010 comprises separating at least part of the solids from the aqueous medium using a centrifuge. According to some embodiments, the step of block 1010 comprises separating at least part of the solids from the aqueous medium using centrifuge 115. According to some embodiments, the step of block 1010 comprises separating at least part of the solids from the aqueous medium using a centrifuge at a rotational rate of about 50 RPM.
• the method further comprises transferring the aqueous medium from the inner centrifugation chamber 114 to the inner UF chamber 124 through the aqueous medium outlet port 118 and the UF inlet port 126. According to some embodiments, the method further comprises transferring the aqueous medium from the inner centrifugation chamber 114 to the inner UF chamber 124 through the centrifuge-UF pipe 1112. According to some embodiments, the method further comprises pumping the aqueous medium from the inner centrifugation chamber 114 to the inner UF chamber 124 through the aqueous medium outlet port 118 and the UF inlet port 126 using the pump. According to some embodiments, the method further comprises pumping the aqueous medium from the inner centrifugation chamber 114 to the inner UF chamber 124 through the centrifuge-UF pipe 1112 using the pump.
• the method further comprises combining the insoluble solids separated in the step of block 1010 with the isolated treated beverage product (block 1100).
• the step of block 1010 further comprises transferring the insoluble solids from the inner centrifugation chamber 114 to the treated beverage container 150, through the solid outlet port 119.
• the method further comprises combining the insoluble solids of the step of block 1010 with the isolated treated beverage product of step (f) (blocks 1050 and 1100).
• the method further comprises transferring the insoluble solids from the inner centrifugation chamber 114 to the treated beverage container 150.
• the method further comprises transferring the insoluble solids from the inner centrifugation chamber 114 to the treated beverage container 150 through the centrifuged solid outlet port 119.
• the method further comprises transferring the insoluble solids from the inner centrifugation chamber 114 to the treated beverage container 150 through the centrifuge-treated beverage container pipe 1115.
• the method further comprises regulating the flow of the insoluble solids from the inner centrifugation chamber 114 to the treated beverage container 150 by the centrifuge-treated beverage container flow valve 251.
• the method comprises transferring the untreated beverage directly to the inner UF chamber 124 through the centrifugation bypass line CBL and the UF inlet port 126.
• Block 1020 shown in Figure 2 relates to the ultrafiltration (UF) of the aqueous medium (or in some embodiments, specifically when the step of block 1010 is not performed, the untreated beverage). This is described in step (b) herein. Specifically, according to some embodiments, step (b) includes ultra-filtering the aqueous medium to produce an ultra-filtered permeate and an ultra-filtered retentate.
• step (b) (block 1020) comprises ultra-filtering the beverage through an ultrafiltration membrane, which has molecular weight cutoff in the range of 5-100 kDa, 5-90 kDa, 5-80 kDa, 5-70 kDa, 5-60 kDa, 5-50 kDa, 5- 40 kDa, 5-30 kDa, 5-25 kDa, 5-20 kDa, 5-15 kDa or 5-10 kDa.
• step (b) (block 1020) comprises ultra-filtering the beverage through an ultrafiltration membrane, which has molecular weight cutoff in the range of 5-10 kilodaltons (kDa).
• step (b) (block 1020) comprises ultra-filtering the beverage at a pressure of about 2 to about 8 Bar, including each value and subrange within the specified range.
• step (b) (block 1020) comprises ultra-filtering the beverage at a pressure of 40 to 100 PSI, 45 to 95 PSI, 50 to 90 PSI, 55 to 85 PSI, 60 to 80 PSI, or 65 to 75 PSI.
• the pressure at the retentate side of the UF filter 125 is in the range of 35 to 95 PSI, 40 to 90 PSI, 45 to 85 PSI, 50 to 80 PSI, 55 to 75 PSI, or 60 to 70 PSI.
• the UF retentate volume flow rate is in the range of 6 to 12, 7 to 11, 8 to 10 or 8.5 to 9.5 liters per minute.
• the UF permeate volume flow rate at the side of UF filter 125, which is distal from the pump is in the range of 1 to 2, 1.25 to 1.75 or 1.4 to 1.6 liters per minute.
• step (b) (block 1020) comprises ultra-filtering by crossflow filtration technique. The beverage can be filtered through the UF filter 125 in multiple filtration cycles while flowing tangentially along one or more UF membranes using the crossflow filtration technique.
• the pump is driven by a Variable Frequency Drive (VFD).
• VFD Variable Frequency Drive
• the pump is operated by a VFD of about 35Hz.
• step (b) is performed in the UF unit 120.
• the ultrafiltration of step (b) is performed by the UF filter 125.
• step (b) produces an ultra-filtered permeate and an ultra-filtered retentate.
• permeate refers to the fraction of the feed that has permeated through the membrane; the permeate is the stream depleted of at least a portion of the retained species.
• retentate refers to the fraction of the liquid composition that has been retained by the membrane; the retentate is the stream enriched in the retained species.
• Block 1021 shown in Figure 2 relates to the UF permeate produced by the ultrafiltration of step (b).
• the UF permeate produced in step (b) has a total sugar concentration of 4 gr to 15 gr, 5 gr to 12 gr, 5.5 gr to 11 gr, or 6.5 gr to 10 gr sugars per 100 gr permeate.
• a total sugar concentration 4 gr to 15 gr, 5 gr to 12 gr, 5.5 gr to 11 gr, or 6.5 gr to 10 gr sugars per 100 gr permeate.
• the total sugars in the UF permeate produced in step (b) comprise disaccharides including sucrose (for example, when the beverage is fruit or vegetable juice), lactose (for example, when the beverage is milk), or maltose(for example, when the beverage is beer), and monosaccharides including one or more of fructose (in juice), galactose (in milk) and/or glucose.
• disaccharides including sucrose (for example, when the beverage is fruit or vegetable juice), lactose (for example, when the beverage is milk), or maltose(for example, when the beverage is beer), and monosaccharides including one or more of fructose (in juice), galactose (in milk) and/or glucose.
• the UF permeate produced in step (b) has a total disaccharide concentration of 2 gr to 8 gr 2.5 gr to 6 gr 3 grto 5 gr or 3.5 grto 4.5 gr disaccharides per 100 gr permeate.
• the disaccharide in the UF permeate produced in step (b) comprises sucrose, lactose, maltose or combinations. Each possibility represents a separate embodiment of the invention.
• the disaccharide in the UF permeate produced in step (b) consist essentially of sucrose.
• the UF permeate in the scenario when the beverage is a fruit or vegetable juice, the UF permeate has a sucrose concentration of 2 gr to 8 gr 2.5 gr to 6 gr 3 gr to 5 gr or 3.5 gr to 4.5 gr sucrose per 100 gr permeate.
• the UF permeate produced in step (b) has a ratio of disaccharides to total sugars of 35% to 65%, 40% to 60% or 45% to 55% w/w.
• the UF permeate has a ratio of sucrose to total sugars of 35% to 65%, 40% to 60% or 45% to 55% w/w.
• the UF permeate has a ratio of sucrose to total sugars of 35% to 65%, 40% to 60% or 45% to 55% w/w.
• the UF permeate produced in step (b) has a ratio of disaccharides to monosaccharides of 1.1 : 1 to 1 : 1.1, 1.25: 1 to 1 : 1.25, 1.5: 1 to 1 : 1.5 or 2: 1 to 1 :2.
• the UF permeate in the scenario when the beverage is a fruit or vegetable juice, has a ratio of sucrose to monosaccharides of 1.1 : 1 to 1 : 1.1, 1.25: 1 to 1 : 1.25, 1.5: 1 to 1 : 1.5 or 2: 1 to 1 :2.
• the UF permeate has a ratio of sucrose to monosaccharides of 1.1 : 1 to 1 : 1.1, 1.25: 1 to 1 : 1.25, 1.5: 1 to 1 : 1.5 or 2: 1 to 1 :2.
• each possibility represents a separate embodiment of the invention.
• the UF permeate in the scenario when the beverage is a fruit or vegetable juice, has a ratio of sucrose to glucose of about 2: 1, 2.5: 1 or 1 : 1 to 3: 1.
• the monosaccharides comprise fructose, glucose, galactose or a combination thereof.
• Each possibility represents a separate embodiment of the invention.
• the UF permeate produced in step (b) comprises beverage organic compounds, which are separated from the corresponding retentate upon their properties and the properties of the UF filter 125.
• the UF permeate produced in step (b) comprises beverage organic compounds, which are permeable to a UF membrane having molecular weight cutoff in the range of: 5-100 kDa, 5-90 kDa, 5- 80 kDa, 5-70 kDa, 5-60 kDa, 5-50 kDa, 5-40 kDa, 5-30 kDa, 5-25 kDa, 5-20 kDa, 5-15 kDa or 5-10 kDa.
• a UF membrane having molecular weight cutoff in the range of: 5-100 kDa, 5-90 kDa, 5- 80 kDa, 5-70 kDa, 5-60 kDa, 5-50 kDa, 5-40 kDa, 5-30 kDa, 5-25 kDa, 5-20 kDa, 5-15 kDa or 5-10 kDa.
• Each possibility represents a separate embodiment of the invention and including each value and sub-range within the specified range.
• the UF permeate produced in step (b) comprises beverage organic compounds, which are permeable to a UF membrane having molecular weight cutoff of 5-10 kilodalton (kDa).
• Natural organic compounds can typically include sugars, proteins, calcium, and fats.
• substantially devoid means that a preparation or composition according to the invention that generally contains less than 20%, less than 15%, less than 10%, less than 5%, less than 3% or less than 1% w/w of the stated substance.
• a preparation or composition according to the invention that generally contains less than 20%, less than 15%, less than 10%, less than 5%, less than 3% or less than 1% w/w of the stated substance.
• the UF permeate produced in step (b) (blocks 1020 and 1021) has Brix in the range of 8% to 12% or 9 to 11%.
• each possibility represents a separate embodiment of the invention.
• the UF permeate produced in step (b) has pH in the range of 2.5 to 4.5 or 3 to 4.
• the UF permeate produced in step (b) has acid content in the range of 0.4% to 0.8% w/w.
• the UF permeate produced in step (b) (blocks 1020 and 1021) has density in the range of 1.035-1.045 gr/ml.
• the UF permeate produced in step (b) (blocks 1020 and 1021) has conductivity in the range of 3700-4700 gr/ml pS.
• the UF permeate produced in step (b) comprises vitamin C in a concentration of 0.1 to 50 mg per 100ml of the permeate.
• the method further comprises transferring the ultra-filtered permeate from the inner UF chamber 124 to the inner NF chamber 134. According to some embodiments, the method further comprises transferring the ultrafiltered permeate from the inner UF chamber 124 to the inner NF chamber 134 through the UF permeate outlet port 128 and the NF inlet port 136. According to some embodiments, the method further comprises transferring the ultra-filtered permeate from the inner UF chamber 124 to the inner NF chamber 134 through the UF-NF pipe 1213. According to some embodiments, the method further comprises regulating the flow of the ultra-filtered permeate from the inner UF chamber 124 to the inner NF chamber 134 by the UF-NF flow valve 213. According to some embodiments, the method further comprises pumping the ultra-filtered permeate from the inner UF chamber 124 to the inner NF chamber 134 using the pump.
• Block 1022 shown in Figure 2 relates to the UF retentate produced by the ultrafiltration of step (b).
• the UF retentate produced in step (b) (blocks 1020 and 1022) comprises beverage organic compounds, which are separated from the corresponding permeate upon their properties and the properties of the UF filter 125.
• the UF retentate produced in step (b) comprises beverage organic compounds, which are impermeable to a UF membrane having molecular weight cutoff in the range of: 5-100 kDa, 5-90 kDa, 5-80 kDa, 5-70 kDa, 5-60 kDa, 5-50 kDa, 5-40 kDa, 5-30 kDa, 5-25 kDa, 5-20 kDa, 5-15 kDa or 5-10 kDa.
• Each possibility represents a separate embodiment of the invention and including each value and sub-range within the specified range.
• the UF retentate produced in step (b) comprises beverage organic compounds, which are impermeable to a UF membrane having molecular weight cutoff of 5-10 kilodalton (kDa).
• the UF retentate produced in step (b) comprises the solids present in the beverage.
• step 1010 is not performed and UF retentate produced in step (b) (blocks 1020 and 1022) comprises 10% to 80% of the solids originally in the beverage, including each value and sub-range within the specified range.
• the UF retentate produced in step (b) has Brix in the range of 10% to 13%, including each value and sub-range within the specified range.
• the UF retentate produced in step (b) (blocks 1020 and 1022) has pH in the range of 3 to 4, including each value and sub-range within the specified range.
• the UF retentate produced in step (b) (blocks 1020 and 1022) has density in the range of 1.040-1.055 gr/ml, including each value and subrange within the specified range.
• the UF retentate produced in step (b) (blocks 1020 and 1022) has conductivity in the range of 4000-5000 pS, including each value and sub-range within the specified range.
• the UF retentate produced in step (b) (blocks 1020 and 1022) has acid content in the range of 0.4% to 1%, including each value and subrange within the specified range.
• the UF retentate produced in step (b) comprises sucrose at a concentration of 4 gr o 5.5 gr per 100 gr retentate, including each value and sub-range within the specified range.
• the UF retentate produced in step (b) comprises glucose at a concentration of 1.7 gr to 2.7 gr per 100 gr retentate, including each value and sub-range within the specified range.
• the UF retentate produced in step (b) comprises fructose at a concentration of 1.9 gr to 2.9 gr per 100 gr retentate, including each value and sub-range within the specified range.
• the UF filter comprises polyether sulfone.
• the UF retentate produced in step (b) comprises vitamin C at a concentration of 0.1 to 50 mg per 100 ml retentate, including each value and sub-range within the specified range.
• the method further comprises step (e), which includes combining the ultra-filtered retentate of step (b) (blocks 1020 and 1022) with the product of step (c) or (d) (dashed arrow from block 1022 to block 1100).
• the method further comprises combining at least some of the ultra-filtered retentate of step (b) (blocks 1020 and 1022) with the isolated treated beverage product of step (f) (dashed arrow from block 1022 to block 1100).
• the method further comprises transferring the ultra-filtered retentate from the inner UF chamber 124 to the treated beverage container 150. According to some embodiments, the method further comprises transferring the ultra-filtered retentate from the inner UF chamber 124 to the treated beverage container 150 through the UF retentate outlet port 129. According to some embodiments, the method further comprises transferring the ultra-filtered retentate from the inner UF chamber 124 to the treated beverage container 150 through the UF-treated beverage container pipe 1215. According to some embodiments, the method further comprises regulating the flow of the ultra-filtered retentate from the inner UF chamber 124 to the treated beverage container 150 by the UF-treated beverage container flow valve 215. According to some embodiments, the method further comprises pumping the ultrafiltered retentate from the inner UF chamber 124 to the treated beverage container 150 using the pump.
• Block 1030 shown in Figure 2 relates to the nanofiltration (NF) of the UF permeate obtained in step (b). This is described in step (c) herein. Specifically, according to some embodiments, step (c) includes nano-filtering the UF permeate obtained in step (b) to produce a nano-filtered permeate and a nano-filtered retentate.
• step (c) (block 1030) comprises nano-filtering the UF permeate through a nanofiltration membrane, which has molecular weight cutoff in the range of 100 - 1000 Dalton, 120 - 800 Dalton, 130 - 700 Dalton, 150 — 500 Dalton, 180 - 500 Dalton, 200 - 500 Dalton, 225 - 500 Dalton 250 - 500 Dalton, 275 - 500 Dalton or 300 - 500 Dalton.
• step (c) (block 1030) comprises nano-filtering the UF permeate through a nanofiltration membrane, which has molecular weight cutoff in the range of 300-500 Daltons.
• step (c) includes nano-filtering the UF permeate through one or more nanofiltration membranes.
• step (c) comprises nano-filtering the UF permeate obtained in step (b) to produce a nanofiltered permeate and a nano-filtered retentate, wherein the nano-filtering is performed through one or more nanofiltration membranes.
• the nano-filtering is performed through a plurality of nanofiltration membranes.
• the nano-filtering is performed through a plurality of nanofiltration membranes, wherein at least one of the nanofiltration membranes has a molecular weight cutoff as defined herein (e.g. in the range of 150-500 or 300-500 Da).
• the nano-filtering is performed through a plurality of nanofiltration membranes, wherein each one of the nanofiltration membranes has a molecular weight cutoff as defined herein (e.g. in the range of 1 SO- SOO or 300-500 Da).
• step (c) comprises nano-filtering at a TMP of at least 10 bar.
• the method further comprises increasing the TMP during at least a part of step (c).
• the TMP can be controlled by the controller described above.
• the TMP can be controlled by controlling a pump facilitating the TMP.
• the TMP can be controlled by controlling one or more valves or other components effecting the TMP.
• the TMP can be increased during a part of or whole of the nanofiltration either continuously or in discrete (periodic or aperiodic) steps time to time.
• the TMP can be increased continuously.
• the TMP can be increased periodically or in discrete steps. According to some embodiments, the TMP can be increased according to a predetermined pattern. According to some embodiments, step (c) (block 1030) comprises nano-filtering by crossflow filtration technique. The beverage can be filtered through the NF filter 135 in multiple filtration cycles while flowing tangentially along one or more NF membranes using the crossflow filtration technique.
• the beverages being treated by the present method and system are complex liquids (juices, milk, beer, etc.) having large molecules, small molecules, suspended compounds, soluble and/or insoluble big molecules, and using high pressures for filtration thereof is not generally expected to render desirable results.
• a higher TMP would be expected to result in poor separation and consequently, higher sugar content in the permeate.
• filtering specifically nano-filtering at a high TMP of at least 10 bar provided the unexpected results of sugar reduction in the NF permeate.
• the brix of the resultant treated beverage again started increasing as the time passed. Thereafter, further increasing the inlet pressure to a further increased value, while not changing any other parameter, the brix value drops again.
• the TMP has to be maintained at a minimum value (for example, at least 10 bar) and/or even to be increased (continuously or in discrete steps) during the nanofiltration process.
• the nanofiltration can be performed at an increasing TMP during at least a part of the filtration step, whereas the increase can be continuous or in discrete steps.
• crossflow filtration technique is also beyond routine choice and yields unexpected results.
• the beverages being treated by the present method and system are complex liquids having big molecules, as well as disaccharides, and using crossflow filtration would not be a routine and/or obvious choice for filtration thereof.
• crossflow filtration would not be a routine and/or obvious choice for filtration thereof.
• the nanofiltration can be performed at a high TMP due to crossflow filtration technique, among other possibilities including performing the nanofiltration at high TMP (as specified herein) without using the crossflow filtration technique.
• the nanofiltration can be performed at a high TMP (as specified herein) without using the crossflow filtration.
• step (c) (block 1030) comprises nano-filtering the UF permeate at a TMP (Trans Membrane Pressure) of 10 to 65 Bar, including each value and sub-range within the specified range.
• the step (c) (block 1030) comprises nano-filtering the UF permeate at a TMP of 10 to 20 Bar, 10 to 30 Bar, 10 to 40 Bar, 10 to 50 Bar, 10 to 60 Bar, 10 to 65 Bar, 15 to 25 Bar, 20 to 30 Bar, 25 to 35 Bar, 30 to 40 Bar, 35 to 45 Bar, 40 to 50 Bar, 45 to 55 Bar, 50 to 60 Bar, or 55 to 65 Bar.
• TMP Trans Membrane Pressure
• step (c) comprises nano-filtering the beverage at a pressure of 150 to 300 PSI, 175 to 250 PSI, 200 to 250 PSI or 200 to 225 PSI.
• the pressure at the retentate side of the NF filter 135 is in the range of 150 to 300 PSI, 175 to 250 PSI, 200 to 250 PSI or 200 to 225 PSI.
• the pressure at the retentate side of the NF filter 135 is in the range of 150 to 300 PSI, 175 to 250 PSI, 200 to 250 PSI or 200 to 225 PSI.
• each possibility represents a separate embodiment of the invention.
• the NF retentate volume flow rate is in the range of 6 to 12, 7 to 11, 8 to 10 or 8.5 to 9.5 liters per minute.
• the NF permeate volume flow rate at the side of NF filter 135, which is distal from the pump is in the range of 2 to 4, 2.5 to 3.5 or 2.8 to 3.2 liters per minute.
• each possibility represents a separate embodiment of the invention.
• step (c) entails application of VFD (Variable Frequency Drive) of about 35Hz to about 40Hz. According to some embodiments, step (c) entails application of VFD (Variable Frequency Drive) of about 40Hz.
• step (c) is performed in the NF unit 130.
• the nanofiltration of step (c) is performed by the NF filter 135.
• step (c) produces a nano-filtered permeate and a nano-filtered retentate.
• Block 1031 shown in Figure 2 relates to the NF permeate produced by the nanofiltration of step (c).
• the NF permeate produced in step (d) has a total sugar concentration of 3 to 6 gr sugars per 100 ml permeate, including each value and sub-range within the specified range.
• the total sugars in the NF permeate produced in step (c) comprises disaccharides including sucrose (for example, when the beverage is fruit or vegetable juice), lactose (for example, when the beverage is milk), or maltose(for example, when the beverage is beer), and monosaccharides including one or more of fructose (in juice), galactose (in milk) and/or glucose.
• sucrose for example, when the beverage is fruit or vegetable juice
• lactose for example, when the beverage is milk
• maltose for example, when the beverage is beer
• monosaccharides including one or more of fructose (in juice), galactose (in milk) and/or glucose.
• the NF permeate produced in step (c) has a total disaccharide concentration of 1 to 2 gr sugars per 100 ml permeate, including each value and subrange within the specified range.
• the disaccharide in the NF permeate produced in step (c) comprises sucrose, lactose, maltose, or combinations. Each possibility represents a separate embodiment of the invention.
• the disaccharide in the NF permeate produced in step (c) comprises sucrose.
• the NF permeate in the scenario when the beverage is a fruit or vegetable juice, has a sucrose concentration of 1 to 2 gr sugars per 100 ml permeate, including each value and subrange within the specified range. According to some embodiments, in the scenario when the beverage is a fruit or vegetable juice, the NF permeate has a ratio of disaccharides to total sugars of 1 : 1 to 1 :8, 1 : 1.5 to 1 :6, 1 :2 to 1 :5 or 1 :2.5 to 1 :5. Each possibility represents a separate embodiment of the invention.
• the NF permeate has a ratio of sucrose to total sugars of 1 : 1 to 1 :8, 1 : 1.5 to 1 :6, 1 :2 to 1 :5 or 1 :2.5 to 1 :5.
• a ratio of sucrose to total sugars of 1 : 1 to 1 :8, 1 : 1.5 to 1 :6, 1 :2 to 1 :5 or 1 :2.5 to 1 :5.
• the NF permeate has a ratio of sucrose to glucose of 1:0.5 to 1 :4, 1 : 1.25 to 1 :3, 1 : 1 to 1 :2.5 or 1 : 1.25 to 1 :2.5.
• the monosaccharides comprise fructose, glucose, galactose or a combination thereof.
• the disaccharide in the NF permeate produced in step (c) comprises lactose.
• the untreated beverage has total sugars including disaccharides comprising lactose.
• the NF permeate produced in step (c) has at least 50% less lactose than the untreated milk provided in step (a) (block 1000).
• the NF permeate produced in step (c) (blocks 1030 and 1031) has 50% to 90% less lactose than the untreated milk provided in step (a) (block 1000), including each value and sub-range within the specified range.
• the NF permeate produced in step (c) (blocks 1030 and 1031) has 80% less lactose than the untreated milk provided in step (a) (block 1000).
• the disaccharide in the NF permeate produced in step (c) comprises maltose.
• the untreated beverage has total sugars including disaccharides comprising maltose, and monosaccharides comprising glucose.
• the NF permeate has at least 30% less total sugars than the untreated beer provided in step (a) (block 1000).
• the NF permeate produced in step (c) (blocks 1030 and 1031) has 30% to 80% less total sugars than the untreated beer provided in step (a) (block 1000), including each value and sub-range within the specified range.
• the NF permeate produced in step (c) comprises beverage organic compounds, which are separated from the corresponding retentate upon their properties and the properties of the NF filter 135.
• the NF permeate produced in step (c) is substantially devoid of beverage organic compounds, which have molecular weight above 150 Dalton, above 180 Dalton, above 200 Dalton, above 250 Dalton, above 275 Dalton, above 300 Dalton, above 400 Dalton, or above 500 Dalton.
• Each possibility represents a separate embodiment of the invention and including each value and sub-range within the specified range.
• the NF permeate is substantially devoid of natural beverage organic compounds, which have molecular weight above 500 Dalton.
• the NF permeate comprises beverage organic compounds, which have molecular weight below 500 Dalton, below 400 Dalton, below 300 Dalton, below 200 Dalton, below 180 Dalton, or below 150 Dalton.
• the NF permeate comprises beverage organic compounds, which have molecular weight below 180 Dalton.
• the NF permeate comprises vitamin C.
• the NF permeate produced in step (c) comprises beverage organic compounds, which are permeable to an NF membrane having molecular weight cutoff in the range of 100 - 1000 Dalton, 120 - 800 Dalton, 130 - 700 Dalton, 150 - 500 Dalton, 180 - 500 Dalton, 200 - 500 Dalton, 225 - 500 Dalton, 250 - 500 Dalton or 300 - 500 Dalton.
• NF membrane having molecular weight cutoff in the range of 100 - 1000 Dalton, 120 - 800 Dalton, 130 - 700 Dalton, 150 - 500 Dalton, 180 - 500 Dalton, 200 - 500 Dalton, 225 - 500 Dalton, 250 - 500 Dalton or 300 - 500 Dalton.
• Each possibility represents a separate embodiment of the invention and including each value and sub-range within the specified range.
• the NF permeate produced in step (c) comprises beverage organic compounds, which are permeable to a UF membrane having molecular weight cutoff of 5-10 kilodalton (kDa) and to an NF membrane having molecular weight cutoff of 300-500 Dalton.
• the NF permeate produced in step (c) (blocks 1030 and 1031) has Brix in the range of 2% to 6% or 2.5% to 5.5%.
• the NF permeate produced in step (c) has Brix in the range of 2% to 6% or 2.5% to 5.5%.
• the NF permeate produced in step (c) has pH in the range of 2.5 to 4.5 or 3 to 4.
• the NF permeate produced in step (c) has acid content in the range of 0.3% to 0.8% w/w, including each value and sub-range within the specified range.
• the NF permeate produced in step (c) (blocks 1030 and 1031) has density in the range of 1.01-1.03 gr/ml, including each value and sub-range within the specified range.
• the NF permeate produced in step (c) (blocks 1030 and 1031) has conductivity in the range of 3000-4500gr/ml pS, including each value and sub-range within the specified range.
• the NF permeate produced in step (c) comprises vitamin C in a concentration of 5 to 50 mg per 100ml of the permeate.
• the NF permeate comprises 50% to 80% less sucrose than the untreated fruit or vegetable juice of step (a), including each value and sub-range within the specified range.
• the method further comprises transferring the nano-filtered permeate from the inner NF chamber 134 to the inner adsorption chamber 144. According to some embodiments, the method further comprises transferring the nano-filtered permeate from the inner NF chamber 134 to the inner adsorption chamber 144 through the NF permeate outlet port 138 and the adsorption inlet port 146. According to some embodiments, the method further comprises transferring the nano- filtered permeate from the inner NF chamber 134 to the inner adsorption chamber 144 through the NF-adsorption pipe 1314.
• the method further comprises regulating the flow of the nano-filtered permeate from the inner NF chamber 134 to the inner adsorption chamber 144 by the NF-adsorption flow valve 314. According to some embodiments, the method further comprises pumping the nano-filtered permeate from the inner NF chamber 134 to the inner adsorption chamber 144 using the pump.
• the method further comprises transferring the nano-filtered permeate from the inner NF chamber 134 directly to the treated beverage container 150 via the adsorption bypass line ABL, while bypassing the adsorption unit 140.
• the solid line can be from block to 1031 to block 1100.
• Block 1032 shown in Figure 2 relates to the NF retentate produced by the nanofiltration of step (c).
• the NF retentate produced in step (c) comprises beverage organic compounds, which are separated from the corresponding permeate upon their properties and the properties of the nanofilter 135.
• the NF retentate produced in step (c) comprises beverage organic compounds, which have molecular weight above any one of the molecular weight cutoffs specified for the nanofilter, but below any one of the molecular weight cutoffs specified for the ultrafilter.
• the NF retentate comprises beverage organic compounds, which have molecular weight in the range of 150 to 20,000 Dalton, 150 to 10,000 Dalton, 150 to 7,500 Dalton, 150 to 5,000 Dalton, 180 to 20,000 Dalton, 180 to 10,000 Dalton, 180 to 7,500 Dalton, 180 to 5,000 Dalton, 200 to 20,000 Dalton, 200 to 10,000 Dalton, 200 to 7,500 Dalton, 200 to 5,000 Dalton, 250 to 20,000 Dalton, 250 to 10,000 Dalton, 250 to 7,500 Dalton, 250 to 5,000 Dalton or 300 to 5,000 Dalton.
• Each possibility represents a separate embodiment of the invention and including each value and sub-range within the specified range.
• the NF retentate produced in step (c) comprises beverage organic compounds, which have molecular weight in the range of about 300 to about 10,000 Dalton.
• the NF retentate is substantially devoid of beverage organic compounds, which have molecular weight above about 5 kilodalton (kDa).
• the NF retentate is substantially devoid of beverage organic compounds, which have molecular weight above about 10 kilodalton (kDa).
• the NF retentate is substantially devoid of beverage organic compounds, which have molecular weight below about 150 Dalton.
• the isolated sugar composition also referred to herein as beverage sugar composition or isolated beverage sugar composition
• the isolated sugar composition is also characterized as above, according to some embodiments.
• the NF retentate produced in step (c) comprises beverage organic compounds, which are impermeable to a NF membrane having molecular weight cutoff in the range of: 100 - 1000 Dalton, 120
• UF membrane having molecular weight cutoff in the range of: 5-100 kDa, 5-90 kDa, 5- 80 kDa, 5-70 kDa, 5-60 kDa, 5-50 kDa, 5-40 kDa, 5-30 kDa, 5-25 kDa, 5-20 kDa, 5-15 kDa or 5-10 kDa.
• Each possibility represents a separate embodiment of the invention and including each value and sub-range within the specified range.
• the NF retentate (as well as the isolated sugar composition of the invention) comprises beverage organic compounds, which are permeable to a UF membrane having molecular weight cutoff of 5-10 kilodalton (kDa), but impermeable to a NF membrane having molecular weight cutoff in the range of 180
• the NF retentate (as well as the isolated sugar composition of the invention) comprises beverage organic compounds, which are permeable to a UF membrane having molecular weight cutoff of 5-10 kilodalton (kDa), but impermeable to a NF membrane having molecular weight cutoff in the range of 300
• the NF retentate produced in step (c) has Brix in the range of 10% to 50%, including each value and subrange within the specified range.
• the NF retentate produced in step (c) has Brix of about 22.5%.
• the NF retentate produced in step (c) (blocks 1030 and 1032) has pH in the range of 3 to 4, including each value and sub-range within the specified range.
• the NF retentate produced in step (c) (blocks 1030 and 1032) has density in the range of 1.01-1.10 gr/ml, including each value and sub-range within the specified range.
• the NF retentate produced in step (c) (blocks 1030 and 1032) has conductivity in the range of 3500-5000 pS, including each value and sub-range within the specified range.
• the NF retentate produced in step (c) (blocks 1030 and 1032) has acid content in the range of 0.3% to 1%, including each value and sub-range within the specified range.
• the NF retentate produced in step (c) comprises sucrose at a concentration of 10 gr to 50 gr per 100 gr retentate, including each value and sub-range within the specified range.
• the NF retentate produced in step (c) comprises glucose at a concentration of 1 gr to 5 gr per 100 gr retentate, including each value and sub-range within the specified range.
• the NF retentate produced in step (c) comprises fructose at a concentration of 1 gr to 5 gr per 100 gr retentate, including each value and sub-range within the specified range.
• the NF retentate produced in step (c) comprises vitamin C at a concentration of 5 to 50 mg per 100 ml retentate, including each value and sub-range within the specified range.
• the NF retentate produced in step (c) comprises total sugars at a concentration of 10 to 50 gr per 100 gr retentate, including each value and sub-range within the specified range.
• the NF retentate produced in step (c) comprises total amino acid content in the range of 0.3% to 1.5%, including each value and sub-range within the specified range.
• the is provided a method for producing an isolated beverage sugar composition from a beverage comprising: (a) providing a beverage; (b) ultra-filtering the aqueous medium through an ultrafiltration membrane, which has molecular weight cutoff in the range of 5-20 kDa to produce an ultra-filtered permeate and an ultra-filtered retentate; (c-i) nano-filtering the ultrafiltered permeate through a nanofiltration membrane, which has molecular weight cutoff in the range of 150-500 Da to produce a nano-filtered permeate and a nanofiltered retentate, wherein the nano-filtered retentate comprises at least part of the beverage sugar; and (c-ii) isolating and optionally drying the beverage sugar of the nano-filtered retentate to produce an isolated beverage sugar composition comprising the beverage sugar.
• the method further comprises transferring the nano-filtered retentate from the inner NF chamber 134 to the isolated sugar composition container 160. According to some embodiments, the method further comprises transferring the nano-filtered retentate from the inner NF chamber 134 to the isolated sugar composition container 160 through the NF retentate outlet port 139. According to some embodiments, the method further comprises transferring the nano-filtered retentate from the inner NF chamber 134 to the isolated sugar composition container 160 through the NF-sugar container pipe 1316. According to some embodiments, the method further comprises regulating the flow of the nano-filtered retentate from the inner NF chamber 134 to the isolated sugar composition container 160 by the NF-sugar container flow valve 316.
• Block 1034 shown in Figure 2 relates to drying and isolating the NF retentate.
• the isolated sugar composition container 160 may include a device configured to dry the isolated sugar composition from residual water. Suitable drying devices include a blower for air/gas flow drying, a heater for promoting evaporation or a vacuum device. Each possibility represents a separate embodiment of the invention.
• step (c- ii) comprises air drying, gas drying, vacuum drying and or heated drying of the nanofiltered retentate. Each possibility represents a separate embodiment of the invention.
• Block 1200 shown in Figure 2 relates to the isolated sugar composition produced by the method of the present invention.
• the isolated fruit or vegetable sugar composition comprises 20 to 40 gr sucrose per 100 gr fruit or vegetable sugar composition.
• the isolated fruit or vegetable sugar composition comprises 5 to 15 gr glucose per 100 gr fruit or vegetable sugar composition.
• the isolated fruit or vegetable sugar composition comprises 5 to 15 gr fructose per 100 gr fruit or vegetable sugar composition.
• the isolated fruit or vegetable sugar composition has Brix in the range of 30% to 70%.
• the isolated beverage sugar composition is prepared by the method of the present invention.
• the present isolated beverage sugar composition for use as a sweetener.
• an isolated beverage sugar composition which comprises beverage organic compounds which are permeable to ultrafiltration but impermeable to nanofiltration; and is substantially devoid of beverage organic compounds which are permeable to nanofiltration.
• the isolated beverage sugar composition is further substantially devoid of beverage organic compounds which are impermeable to ultrafiltration.
• the fruit is selected from the group consisting of citrus fruits, apple, apricot, banana, blackberry, blueberry, cherry, cranberry, grape, guava, mango, passion fruit, papaya, peach, pineapple, coconut, plum, pear, pomegranates and raspberry.
• the fruit is a citrus fruit.
• the citrus fruit is selected from the group consisting of: orange, grapefruit, citron, clementine, lemon and tangerine.
• the fruit is orange or grapefruit.
• the fruit is orange.
• the fruit is grapefruit.
• the fruit is apple.
• the fruit is apple.
• an isolated citrus fruit sugar composition which comprises citrus juice organic compounds which are permeable to ultrafiltration but impermeable to nanofiltration; and is substantially devoid of citrus juice organic compounds which are permeable to nanofiltration.
• the isolated citrus fruit sugar composition is further substantially devoid of citrus juice organic compounds which are impermeable to ultrafiltration. According to some embodiments, the isolated citrus fruit sugar is prepared by the method of the present invention.
• Block 1040 shown in Figure 2 relates to the zeolite adsorption of the NF permeate obtained in step (c). This is described in optional step (d) herein.
• step (d) comprises contacting at least one adsorbent with the nano-filtered permeate to produce an adsorbed composition and a treated beverage product.
• step (d) includes contacting the at least one adsorbent with the centrifuged nano-filtered permeate to produce an adsorbed composition and a treated beverage product.
• step (d) is performed in the adsorption unit 140.
• the method of the present invention throughout the UF, NF and adsorption steps was surprisingly found to maintain the large majority of vitamin C in the permeate or in the UF retentate, while substantially reducing the sucrose (and other sugars) content, according to some embodiments.
• vitamin C is not adsorbable to the at least one adsorbent.
• the at least one adsorbent is described above when discussing the system 100, and it is designated the at least one adsorbent 145. Therefore, the relevant embodiment relating to the at least one adsorbent 145 similarly apply for the methods of the present invention.
• the at least one adsorbent comprises a zeolite. According to some embodiments, the at least one adsorbent being active so as to have a higher relative selectivity for disaccharides than for monosaccharides. According to some embodiments, the at least one adsorbent being active so as to have a higher relative selectivity for disaccharides than for organic acids. According to some embodiments, disaccharides comprise sucrose, lactose, maltose or combinations, and the monosaccharides comprise fructose, glucose, galactose or a combination thereof. Each possibility represents a separate embodiment of the invention.
• step (d) comprises passing the nano-filtered permeate though a column comprising the at least one adsorbent to produce an adsorbed composition within the column and a treated beverage product exiting the column.
• Zeolites, in powder or granular form include, for example, strong dealuminated zeolites and NaX type zeolites.
• Zeolites include, for example, Zeolite Y (Type Y Zeolites) compositions, for example, including: Z-5: zeolite Y hydrogen powder with surface area of 730m 2 /g and at SiO2:AhO3 molar ratio of 5: 1, commercially available as Alfa Aesar 45866; Z-30: zeolite Y hydrogen powder and with surface area of 780m 2 /g and SiO2:Ah03 molar ratio of 30: 1, commercially available as Alfa Aesar 45870; and, Z-80: zeolite Y hydrogen powder and with surface area of 780m 2 /g and SiCh: AI2O3 molar ratio of 80: 1, commercially available as Alfa Aesar 45866.
• Z-5 zeolite Y hydrogen powder with surface area of 730m 2 /g and at SiO2:AhO3 molar ratio of 5: 1, commercially available as Alfa Aesar 45866
• Z-30 zeolite Y hydrogen powder and with surface
• Y Zeolites Type Y Zeolites
• Y Zeolite H + Hydrogenated
• Y Zeolite Na Sodium
• Y Zeolite K Panassium
• Y Zeolite Ca Calcium
• the zeolite is selected from zeolites having a Si/Al molar ratio of at least 10: 1. According to some embodiments, the zeolite comprises at least one of Y Zeolite H + and Y Zeolite Ca.
• step (d) is performed in the adsorption unit 140.
• the adsorption of step (d) is performed on the at least one adsorbent 145.
• step (d) is performed at a pressure of about 1 to about 10 Bar, including each value and sub-range within the specified range.
• step (d) produces an adsorbed fraction (block 1042) a non-adsorbed fraction (block 1041).
• Block 1042 shown in Figure 2 relates to the fraction adsorbed in the adsorbent in step (d).
• the adsorbed fraction produced in step (d) comprises beverage organic compounds, which are separated from the corresponding non-adsorbed fraction upon their properties and the properties of the at least one adsorbent 145.
• the adsorbed fraction produced in step (d) comprises beverage organic compounds, which are adsorbed to the at least one adsorbent 145.
• the adsorbed fraction produced in step (d) comprises beverage organic compounds, which are: impermeable to a NF membrane having molecular weight cutoff in the range of:
• UF membrane having molecular weight cutoff in the range of: 5-100 kDa, 5-90 kDa, 5-80 kDa, 5-70 kDa, 5-60 kDa, 5-50 kDa, 5-40 kDa, 5-30 kDa, 5-25 kDa, 5-20 kDa, 5-15 kDa or 5-10 kDa; and which are adsorbable to the at least one adsorbent 145.
• Each possibility represents a separate embodiment of the invention and including each value and subrange within the specified range.
• the adsorbed fraction comprises beverage organic compounds, which are permeable to a UF membrane having molecular weight cutoff of 5-10 kilodalton (kDa), but impermeable to a NF membrane having molecular weight cutoff in the range of 180 - 500 Dalton and are adsorbable to the at least one adsorbent 145.
• beverage organic compounds which are permeable to a UF membrane having molecular weight cutoff of 5-10 kilodalton (kDa), but impermeable to a NF membrane having molecular weight cutoff in the range of 180 - 500 Dalton and are adsorbable to the at least one adsorbent 145.
• the adsorbed fraction comprises beverage organic compounds, which are permeable to a UF membrane having molecular weight cutoff of 5-10 kilodalton (kDa), but impermeable to a NF membrane having molecular weight cutoff in the range of 300 - 500 Dalton and are adsorbable to the at least one adsorbent 145.
• beverage organic compounds which are permeable to a UF membrane having molecular weight cutoff of 5-10 kilodalton (kDa), but impermeable to a NF membrane having molecular weight cutoff in the range of 300 - 500 Dalton and are adsorbable to the at least one adsorbent 145.
• the adsorbed fraction is also referred herein as adsorbed composition.
• the adsorbed composition produced in step (d) (blocks 1040 and 1042) has Brix in the range of 0.5% to 4%, including each value and sub-range within the specified range.
• the adsorbed composition produced in step (d) comprises sucrose at a concentration of 0.5 gr to 2 gr per 100 gr adsorbed composition, including each value and sub-range within the specified range.
• the adsorbed composition produced in step (d) comprises glucose at a concentration of 0 gr to 1 gr per 100 gr adsorbed composition, including each value and sub-range within the specified range.
• the adsorbed composition produced in step (d) comprises fructose at a concentration of 0 gr to 1 gr per 100 gr adsorbed composition, including each value and sub-range within the specified range.
• Block 1041 shown in Figure 2 relates to the non-adsorbed fraction produced by the adsorption of step (d).
• the non-adsorbed fraction is also referred herein as adsorption filtrate.
• the non-adsorbed fraction produced in step (d) has a total sugar concentration in the range of 1 gr to 5.5 gr per 100 ml of the non-adsorbed fraction, including each value and sub-range within the specified range.
• the total sugars in the non-adsorbed fraction produced in step (d) (blocks 1040 and 1041) comprise disaccharides including sucrose, lactose, and/or maltose and monosaccharides including fructose, galactose, and/or glucose. Each possibility represents a separate embodiment of the invention.
• the non-adsorbed fraction produced in step (d) has a total disaccharide concentration in the range of 0 gr to 1.5 gr per 100 ml of the non-adsorbed fraction, including each value and sub-range within the specified range.
• the disaccharides in the non-adsorbed fraction comprise sucrose.
• the non-adsorbed fraction has a sucrose concentration in the range of 0 gr to 1.5 gr per 100 ml of the non-adsorbed fraction, including each value and sub-range within the specified range.
• the nonadsorbed fraction has a ratio of disaccharides to total sugars of 1 :2 to 1 : 100, including each value and sub-range within the specified range.
• the nonadsorbed fraction has a ratio of sucrose to total sugars of 1 :2 to 1 : 100, including each value and sub-range within the specified range.
• the non- adsorbed fraction has Brix in the range of 1% to 5%, including each value and subrange within the specified range.
• the non-adsorbed fraction produced in step (d) has a ratio of disaccharides to monosaccharides of 1 :4 to 1 : 100, including each value and sub-range within the specified range.
• the non-adsorbed fraction has a ratio of sucrose to monosaccharides of 1 :4 to 1 : 100, including each value and sub-range within the specified range.
• the non-adsorbed fraction has a ratio of sucrose to glucose of 1 :6 to 1 : 100, including each value and sub-range within the specified range.
• the non-adsorbed fraction produced in step (d) comprises beverage organic compounds, which are separated from the corresponding adsorbed fraction upon their properties and the properties of the at least one adsorbent 145.
• the non-adsorbed fraction is substantially devoid of beverage organic compounds, which are adsorbable to the at least one adsorbent 145.
• the liquid material has already undergone both UF and NF filtration, maintaining the permeates.
• the non-adsorbed fraction produced in step (d) is (i) substantially devoid of beverage organic compounds, which are adsorbable to the at least one adsorbent 145; and (ii) substantially devoid of beverage organic compounds, which have molecular weight above 150 Dalton, above 180 Dalton, above 200 Dalton, above 250 Dalton, above 300 Dalton, above 400 Dalton, or above 500 Dalton.
• the non-adsorbed fraction comprises beverage organic compounds, which have molecular weight below 500 Dalton and are non-adsorbable to the at least one adsorbent 145.
• non-adsorbed fraction refers to the treated beverage product of step (d).
• the method further comprises transferring the treated beverage product of step (d) from the inner adsorption chamber 144 to the treated beverage container 150.
• the method further comprises transferring the treated beverage product of step (d) from the inner adsorption chamber 144 to the treated beverage container 150 through the treated beverage outlet port 149.
• the method further comprises transferring the treated beverage product of step (d) from the inner adsorption chamber 144 to the treated beverage container 150 through the adsorption- treated beverage pipe 1415.
• the method further comprises regulating the flow of the treated beverage product of step (d) from the inner adsorption chamber 144 to the treated beverage container 150 by the adsorption-treated beverage flow valve 415.
• the method further comprises pumping the treated beverage product of step (d)from the inner adsorption chamber 144 to the treated beverage container 150 using the pump.
• the steps of the blocks 1040, 1041, and 1042 are not performed, and the NF permeate is directly fed to the treated beverage container 150 via the adsorption bypass line ABL, as described above.
• Block 1050 shown in Figure 2 relates to the isolation of the nano-filtered permeate of step (c), the adsorption filtrate of step (d) or the addition product of step (e) as an isolated treated beverage product. This is described in step (f) herein. Specifically, according to some embodiments, step (f) comprises isolating the nanofiltered permeate of step (c), the adsorption filtrate of step (d) or the addition product of step (e) as an isolated treated beverage product.
• Block 1100 shown in Figure 2 relates to the treated beverage product.
• the treated beverage product of the present invention comprises the nano-filtered permeate of step (c), the adsorption filtrate of step (d) or the addition product of step (e) upon the isolation step (f).
• compositions and characteristics of the nano-filtered permeate of step (c), the adsorption filtrate of step (d) or the addition product of step (e) are as detailed herein.
• the isolated treated beverage product comprises at least 30%, at least 35%, at least 40%, at least 45%, at least 50% w/w, at least 55% w/w, or at least 60% w/w less sugar than the untreated beverage provided in step (a).
• the isolated treated beverage product comprises at least 75%, at least 80% w/w, at least 85% w/w, or at least 90% w/w less sucrose than the untreated fruit or vegetable juice of step (a).
• the isolated treated beverage product comprises at least 75%, at least 80% w/w, at least 85% w/w, or at least 90% w/w less sucrose than the untreated fruit or vegetable juice of step (a).
• the isolated treated beverage product comprises at least 75%, at least 80% w/w, at least 85% w/w, or at least 90% w/w less sucrose than the untreated fruit or vegetable juice of step (a).
• Each possibility represents a separate embodiment of the invention.
• the isolated treated beverage product comprises the product provided upon performing steps (a)-(c), (f) and optionally (d) and/or (e).
• the composition of the isolated treated beverage product is as described above for the product of step (c), (d) or (e) after performing step (f).
• the isolated treated beverage product comprises the combination of (i) the product provided upon performing steps (a)-(c), (f) and optionally (d) and/or (e); and (ii) the UF retentate of the beverage.
• the isolated beverage product is substantially devoid of beverage organic compounds, which are adsorbable to the at least one adsorbent 145.
• the isolated beverage product comprises beverage organic compounds, which are non-adsorbable to the at least one adsorbent 145.
• the isolated beverage product is substantially devoid of beverage organic compounds, having molecular weight in the range of 150 to 20,000 Dalton, 150 to 10,000 Dalton, 150 to 7,500 Dalton, 150 to 5,000 Dalton, 180 to 20,000 Dalton, 180 to 10,000 Dalton, 180 to 7,500 Dalton, 180 to 5,000 Dalton, 200 to 20,000 Dalton, 200 to 10,000 Dalton, 200 to 7,500 Dalton, 200 to 5,000 Dalton, 250 to 20,000 Dalton, 250 to 10,000 Dalton, 250 to 7,500 Dalton, 250 to 5,000 Dalton, 300 to 20,000 Dalton, 300 to 10,000 Dalton, 300 to 7,500 Dalton or 300 to 5,000 Dalton.
• the isolated beverage product is substantially devoid of beverage organic compounds, having molecular weight in the range of about 300 Dalton to about 5,000 Dalton.
• the isolated beverage product comprises beverage organic compounds, having molecular weight below 150 Dalton, below 180 Dalton, below 200 Dalton, below 250 Dalton or below 300 Dalton. Each possibility represents a separate embodiment of the invention. According to some embodiments, the isolated beverage product comprises beverage organic compounds, having molecular weight above 5,000 Dalton, above 6,000 Dalton, above 7,000 Dalton or above 8,000 Dalton. Each possibility represents a separate embodiment of the invention. According to some embodiments, the isolated beverage product comprises beverage organic compounds, having molecular weight below 150 Dalton, below 180 Dalton, below 200 Dalton, below 250 Dalton or below 300 Dalton and beverage organic compounds having molecular weight above 5,000 Dalton, above 6,000 Dalton, above 7,000 Dalton or above 8,000 Dalton.
• the isolated beverage product comprises beverage organic compounds that are (i) non-adsorbable to the at least one adsorbent 145, (ii) having molecular weight below 300 Dalton, and (iii) having molecular weight above 5,000 Dalton; and is substantially devoid of beverage organic compounds that are (i) adsorbable to the at least one adsorbent 145, and (ii) having molecular weight in the range of about 300 Dalton to about 5,000 Dalton.
• the isolated beverage product comprises beverage organic compounds that are, (i) having molecular weight below 300 Dalton, and (ii) having molecular weight above 5,000 Dalton; and is substantially devoid of beverage organic compounds that have molecular weight in the range of about 300 Dalton to about 5,000 Dalton.
• the isolated treated beverage product is an isolated reduced-sugar citrus fruit or vegetable juice.
• the isolated treated beverage product is an isolated reduced-sugar citrus fruit or vegetable juice
• the citrus fruit or vegetable juice is selected from the group consisting of: orange juice, grapefruit juice and both.
• the untreated fruit or vegetable juice has an initial Brix/acidity ratio
• the isolated treated fruit or vegetable juice has a treated Brix/acidity ratio which is at least 10% lower than the initial Brix/acidity ratio.
• the isolated treated fruit or vegetable juice has a Brix/acidity ratio in the range of 8.5- to 18.5, including each value and sub-range within the specified range.
• isolated treated fruit juice further includes fruit juice pulp.
• isolated treated fruit juice further includes fruit juice pulp derived from the same fruit. It is to be understood that “derived from the same fruit refers to the plant genus and not necessarily to the same specific fruit. For example, pulp derived from a first orange (or number of fruits) may be incorporated into the isolated treated fruit juice derived from a second orange (or number of fruits).
• the method further comprises in step (e) adding fruit juice pulp to the nano-filtered permeate or to the adsorption filtrate.
• the method further comprises in step (e) adding an untreated beverage to at least at least a portion of the treated beverage.
• the at least a portion of the isolated treated beverage is mixed with the untreated portion of the beverage, such that the end product comprises at least 10% by volume of the untreated portion of the beverage.
• step (e) comprises adding to the isolated treated beverage an additive selected from the group consisting of: a bitterness masking agents, a sweetener, a preservative or any combination thereof.
• the bitterness masking agent comprises a natural extract selected from the group consisting of: cinnamon, chocolate, vanilla, strawberry, coconut, ginger, licorice and a combination thereof.
• the sweetener is a carbohydrate or proteinbased sweetener.
• the sweetener is selected from the group consisting of: date, Stevia, agave fruit, honey, apple, Erythritol, Sweetango, maple, Incredo (Douxmatok), sweelinTM (Amai)and a combination thereof.
• the sweetener comprises Incredo (Douxmatok), sweelinTM (Amai), or both.
• Incredo by Douxmatok is known in the art, and it is an artificial sweetener comprising a modified carbohydrate, sweelinTM by Amai is known in the art, and it is a sweetener comprising a sweet protein.
• the method further comprises mixing the isolated treated beverage with the NF retentate and/or the solids.
• the method further comprises adjusting the pH of the isolated treated beverage.
• the isolated treated beverage further comprises a pH adjusting agent.
• the method further comprises aseptically filling packets with the isolated treated beverage.
• a reduced-sugar beverage prepared according to the method of the present invention. It is to be understood that the “reduced-sugar beverage” refers to the composition of the isolated treated beverage.
• a reduced-sugar beverage comprising: beverage organic compounds which are permeable to ultrafiltration and nanofiltration; and is substantially devoid of: beverage organic compounds which are permeable to ultrafiltration but impermeable to nanofiltration, beverage compounds which are permeable to ultrafiltration and nanofiltration, wherein the ultrafiltration and nanofiltration are as described in any one of the embodiments of the present invention.
• a reduced-sugar beverage comprising: beverage organic compounds which are permeable to ultrafiltration, nanofiltration and zeolite adsorption; and is substantially devoid of: beverage organic compounds which are permeable to ultrafiltration but impermeable to nanofiltration, beverage compounds which are permeable to ultrafiltration and nanofiltration but impermeable to zeolite adsorption, wherein the zeolite has higher relative selectivity for disaccharides than for monosaccharides and, optionally, for organic acids.
• the embodiment directed to the reduced-sugar beverage can be appreciated in light of the embodiments directed to methods and product, which generally describe beverages.
• the embodiments directed to reduced-sugar beverage may refer to any one of the specific beverages specified herein and to combinations thereof.
• the beverage is a citrus fruit juice and the citrus fruit juice is selected from the group consisting of: orange juice, grapefruit juice and both. Each possibility represents a separate embodiment of the invention.
• the beverage further comprises beverage compounds which are impermeable to ultrafiltration.
• the treated beverage further comprises solids extracted from the untreated beverage.
• the reduced-sugar beverage further comprises an additive selected from the group consisting of: a bitterness masking agents, a sweetener, a preservative or any combination thereof. Each possibility represents a separate embodiment of the invention.
• the ultrafiltration is conducted with an ultrafiltration membrane, which has molecular weight cutoff in the range of 5-20 kDa.
• the nanofiltration is conducted with a nanofiltration membrane, which has molecular weight cutoff in the range of 180-500 Da.
• the nanofiltration is conducted with a nanofiltration membrane, which has molecular weight cutoff in the range of 300-500 Da.
• a method for producing a concentrate of a reduced sugar beverage comprising: (a) providing a beverage; (b) ultra-filtering the beverage through an ultrafiltration membrane, which has molecular weight cutoff in the range of 5-20 kDa to produce an ultra-filtered permeate and an ultra-filtered retentate; (c) nano-filtering the ultra-filtered permeate through a nanofiltration membrane, at a TMP (Trans Membrane Pressure) of at least 10 Bar, wherein the nanofiltration membrane has molecular weight cutoff in the range of 150-500 Da to produce a nano-filtered permeate and a nano-filtered retentate; (d) optionally contacting at least one adsorbent with the nano-filtered permeate to produce an adsorbed composition and a liquid medium, and filtering the adsorbed composition from liquid medium to form an adsorption filtrate, wherein the at least one adsorbent comprises a zeolite, and wherein the at least one a
• the steps (a) to (f) correspond to the steps (a) to (f) of any of the methods described herein and can be performed according to any of the embodiments of the methods described herein.
• the isolated treated beverage can be the NF permeate.
• the isolated treated beverage can be the adsorbent filtrate.
• the isolated treated beverage can be the addition product of step (e).
• the beverage can be any of the beverages described herein, and concentrating the treated beverage into a concentrate thereof provides a more commercially viable product. For instance, the concentrate can be stored and transported more conveniently than the beverage itself.
• the concentrate of a reduced sugar beverage comprises a concentrate of a reduced sugar fruit or vegetable juice.
• step (g) includes eliminating a certain amount of water content from the treated beverage to achieve the desired concentrate.
• a concentrate of a reduced sugar beverage prepared by the method of any one of the embodiments described herein.
• the concentrate has a treated Brix/acidity ratio which is at least 5% lower than the initial Brix/acidity ratio of a corresponding concentrate of the untreated beverage provided in step (a). According to some embodiments, the concentrate has a treated Brix/acidity ratio which is at least 8% lower than the initial Brix/acidity ratio of a corresponding concentrate of the untreated beverage provided in step (a).
• a corresponding concentrate of the initially provided beverage in step (a) has a brix/acidity ratio of 10 to 17.
• the final concentrate product has a brix/acidity ratio of 10 to 15.
• a concentrate of a reduced sugar fruit or vegetable juice which has Brix of up to 65% a brix/acidity ratio of 10 to 15%, including each value and sub-range within the specified range.
• the Brix and/or brix/acidity ratio of the concentrate of the reduced sugar fruit or vegetable juice depends on the fruit or vegetable juice that it has been prepared from and/or the Brix and/or brix/acidity ratio of the untreated juice initially provided.
• the fruit or vegetable juice is a citrus fruit juice and the citrus fruit juice is selected from the group consisting of: orange juice, grapefruit juice and both. Each possibility represents a separate embodiment of the invention.
• Example 1 preparation of a reduced sugar orange juice
• Example 1A ultrafiltration The following steps were taken:
• Example IB nanofiltration • Assemble the filtration system with NF membrane with an MWCO of 300- 500Da.
• Example 1C adsorption
• Example IE Natural orange sugar - Concentration of NF retentate
• Example 2 preparation of a reduced sugar orange juice
• Example 3 preparation of a reduced sugar lactose milk.
• Example 3A ultrafiltration (UF) process.
• Example 3 A Ultra-filtration (UF) Process.
• Example 4 preparation of a reduced sugar beer.
• Example 4A ultrafiltration (UF) process.
• Example 4C Final Beer product preparation.

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