WO2009043882A1 - Procédé et installations permettant d'obtenir du lait à faible teneur glucidique - Google Patents

Procédé et installations permettant d'obtenir du lait à faible teneur glucidique Download PDF

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Publication number
WO2009043882A1
WO2009043882A1 PCT/EP2008/063165 EP2008063165W WO2009043882A1 WO 2009043882 A1 WO2009043882 A1 WO 2009043882A1 EP 2008063165 W EP2008063165 W EP 2008063165W WO 2009043882 A1 WO2009043882 A1 WO 2009043882A1
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WO
WIPO (PCT)
Prior art keywords
ultrafiltration
milk
nanofiltration
permeate
content
Prior art date
Application number
PCT/EP2008/063165
Other languages
English (en)
Inventor
Francesco Vernazza
Original Assignee
Parmalat Spa
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Parmalat Spa filed Critical Parmalat Spa
Priority to CA2701066A priority Critical patent/CA2701066C/fr
Priority to AU2008306878A priority patent/AU2008306878B2/en
Publication of WO2009043882A1 publication Critical patent/WO2009043882A1/fr

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Classifications

    • 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; MAKING 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
    • A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; MAKING THEREOF
    • A23C2210/00—Physical treatment of dairy products
    • A23C2210/20—Treatment using membranes, including sterile filtration
    • A23C2210/206—Membrane filtration of a permeate obtained by ultrafiltration, nanofiltration or microfiltration

Definitions

  • the present invention concerns a method, and the relative plant, to obtain milk with low sugar content, reducing or eliminating the lactose naturally present in the milk.
  • lactose is a disaccharide naturally present in the composition of milk, to about 5% in weight.
  • Lactose may entail difficulties in digestion or other problems connected to its metabolization in some categories of consumers, for example people intolerant of lactose or following a course of antibiotics.
  • the hydrolysis determines the conversion of more than 80% of the lactose into monosaccharides, or simple sugars, glucose and galactose.
  • the enzymatic hydrolysis is often combined with other separation methods, such as membrane filtering, chromatography or others.
  • Another disadvantage is that the simple sugars produced in hydrolysis cause a taste that may be too sweet for some categories of consumers, and may be unadvisable in diets with low calorie consumption or for those suffering from disturbances in their sugar metabolism.
  • Purpose of the present invention is to perfect a method and make a relative plant to obtain milk with low sugar content, and particularly lactose, or substantially sugar-free and/or lactose-free, which is quick to execute, flexible to manage, which also has limited costs and which at the same time allows to obtain milk which does not taste too sweet.
  • the method according to the present invention can be used to obtain milk with low sugar content, starting from milk.
  • the initial milk may be raw milk or milk previously heat treated and possibly standardized to a content of fat comprised between the natural value and a substantially zero value.
  • the method according to the present invention comprises at least the following steps: - a first step in which the milk is subjected to ultrafiltration in order to produce, at exit, an ultrafiltration permeate, with a content of dry matter based on milk salts and sugars, and an ultrafiltration retentate; and
  • the nanofiltration permeate is recircled directly to ultrafiltration, so as to re-integrate the milk salts and dilute the content of dry matter of the milk which is subjected to ultrafiltration, consequently reducing the content of dry matter of the ultrafiltration retentate from which the milk with low sugar content is obtained.
  • the dilution of the content of dry matter of the milk subjected to ultrafiltration is at the expense of the sugars.
  • the method according to the present invention allows to obtain milk with low sugar content and particularly low lactose content, or substantially lactose-free.
  • the present invention Since it operates substantially continuously, the present invention needs no intermediate storage, thus reducing plant costs, management costs and the cost of controlling the various steps. Furthermore, the production times are optimized, since there are no serial passages.
  • the present invention allows an extremely elastic production since it allows to decide at any moment how much finished product to produce, when to start and when to finish production. This gives considerable advantages in management and the possibility to reply effectively to sudden requirements to change production.
  • the present invention allows to determine a desired sugar content, but in any case low, in the final product, so as to adapt to the different dietary requirements of consumers.
  • the present invention also allows to obtain, in a rapid manner, milk in which, once the lactose has been reduced, other sugars are substantially not present.
  • the first and the second steps are performed substantially concurrently, advantageously in time and place, and provide to feed the milk continuously to ultrafiltration, and to collect the ultrafiltration retentate continuously, which represents the final product with reduced or zero sugar - A -
  • An advantageous variant of the present invention provides that the content of dry matter of the ultrafiltration retentate is regulated at least by controlling the content of dry matter of the ultrafiltration permeate and the content of dry matter of the nanofiltration permeate.
  • the content of dry matter of the ultrafiltration retentate is also regulated by controlling the flow rates of the streams entering and exiting ultrafiltration and nanofiltration.
  • a plant according to the present invention to obtain milk with low sugar content starting from milk comprises at least an ultrafiltration unit able to produce at exit an ultrafiltration permeate, whose content of dry matter is based on milk salts and sugars, and an ultrafiltration retentate, and a nanofiltration unit able to produce at exit a nanofiltration permeate whose content of dry matter is based on milk salts, and a nanofiltration concentrate with a content of dry matter based on milk sugars.
  • the plant also comprises means to feed and collect liquid, said means being able to feed continuously a stream of milk to the ultrafiltration unit, a stream of ultrafiltration permeate to the nanofiltration unit and a stream of water to the nanofiltration unit and able to continuously collect a stream of the ultrafiltration retentate from the ultrafiltration unit and a stream of nanofiltration concentrate from the nanofiltration unit.
  • the plant also comprises recircling means able to continuously recircle the stream of nanofiltration permeate to the ultrafiltration unit, so as to reintegrate the milk salts and to dilute the content of dry matter of the milk subjected to ultrafiltration, thus reducing the content of dry matter of the ultrafiltration retentate and obtaining the milk from the latter.
  • a variant of the present invention also provides the enzymatic hydrolysis of the milk, before or after the ultrafiltration and nanofiltration operations.
  • hydrolysis performed before the subsequent first and second steps are performed on milk with low lactose content, but with a determinate content of glucose and galactose which are in any case reduced or eliminated thanks to the ultrafiltration and nanofiltration and the relative recircling of the nanofiltration permeate according to the present invention.
  • the milk obtained as final product can also be integrated, or not, with salts deriving from whey, or also possibly from milk, in order to balance the final taste and savor.
  • a method according to the present invention is used to process milk, indicated by the reference M, having a typical initial composition of about 5% in weight of lactose, about 0.7% in weight of salts, milk proteins comprised between about 3% and 4% in weight, and also a fat content comprised between about 0% (skimmed milk) and 4% in weight.
  • a first step of the method provides to feed the milk M continuously to an ultrafiltration unit UF in order to subject it to ultrafiltration, from which an ultrafiltration permeate UFP is obtained, and an ultrafiltration retentate UFR.
  • the present invention provides to standardize the content of fat upstream of the enzymatic hydrolysis, shown by block S, in order to take it to the desired percentage, by means of known techniques.
  • the lactose and the salts pass into the ultrafiltration permeate UFP in equal proportion to that of the milk from which the UFP permeate derives, since the membranes of the ultrafiltration UF are not able to hold them back.
  • the lactose and salts constitute the dry matter, indicated hereafter by the abbreviation d.m., of the ultrafiltration permeate UFP.
  • the ultrafiltration membranes UF are able to hold back the insoluble proteins, typically casein, which remain in the retentate UFR.
  • the ultrafiltration permeate UFP is fed continuously to a nanofiltration unit NF to be subjected to nanofiltration, in order to obtain a relative nanofiltration concentrate NFC which, under normal working conditions, is continuously collected, and a nanofiltration permeate NFP.
  • the nanofiltration NF membranes separate a large part of the lactose and the soluble proteins which go to the concentrate NFC, while substantially all the salts pass to the permeate NFP.
  • the method according to the present invention is based on the concept of reducing to a desired value the value of d.m., and hence lactose, of the ultrafiltration retentate UFR, by diluting the value of d.m. of the stream which is subjected to ultrafiltration UF, performed by the nanofiltration permeate NFP.
  • the reduction in the d.m. value of the ultrafiltration permeate UFP is directly correlated to the reduction in the d.m. value of the retentate UFR. Therefore, controlling the d.m. value of the ultrafiltration permeate UFP is equivalent, based on suitable calculations and/or conversions, to controlling the d.m. value of the retentate UFR.
  • the nanofiltration permeate NFP is used to gradually dilute the stream that is subjected to ultrafiltration UF, and hence the two outlet streams, the permeate UFP and the retentate UFR, until, based on the control of some significant process parameters, the retentate UFR exiting from ultrafiltration has the desired properties for the milk as final product, indicated by LFM.
  • nanofiltration permeate NFP is recircled directly to ultrafiltration UF, while the nanofiltration concentrate NFC is continuously eliminated as a sub-product.
  • Recircling is allowed by at least a pipe D, which connects the nanofiltration NF to the ultrafiltration UF and is provided with a recircling valve VFM, which will be described more fully later.
  • the stream actually subjected to ultrafiltration UF is given by the sum of the streams of milk M and the stream of the nanofiltration permeate NFP.
  • the ultrafiltration retentate UFR is continuously taken from the ultrafiltration unit UF, re-diluted by the stream of nanofiltration permeate NFP, which makes up the final product LFM.
  • a stream of water W is continuously fed to nanofiltration NF, in order to respect the balance of material in its stationary state.
  • the stream actually subjected to nanofiltration N is given by the sum of the streams of water W and the stream of ultrafiltration permeate UFP.
  • the method according to the present invention provides to set the following ratios between the different flow rates:
  • the ratio between the flow rate of the recircled nanofiltration permeate NFP and the flow rate of the ultrafiltration permeate UFP is equal to about 1;
  • the ratio between the flow rate of water W added to nanofiltration NF and the flow rate of the nanofiltration concentrate NFC extracted from nanofiltration is equal to about 1 ;
  • the flow rate of nanofiltration permeate NFP that is recircled is such that its ratio with the flow rate of milk M fed to ultrafiltration UF is comprised between about 1 and 6, preferably between 3 and 5.
  • the recircling of the nanofiltration permeate NFP is advantageous due to the desired dilution, since it is typically a stream with a high content of water with a low content of d.m., substantially consisting of milk salts. Therefore, the recircling brings the necessary diluting water and does not bring lactose to the ultrafiltration UF, but only salts. Therefore, we have a continuous re-integration of the salts present in the ultrafiltration permeate UFP, although diluted, to the ultrafiltration unit UF, preventing or drastically reducing any external re- integrations or additions of salts from other sources to the final product.
  • the parameters that are controlled in the method according to the present invention are the d.m. values of the following streams:
  • the parameters are measured, for example, by measuring the brix.
  • the blocks relating to three dry matter sensors are indicated by DMS, able to measure the content of dry matter of the various streams concerned.
  • the flow rates set for the various streams must guarantee that the control parameters described above, under normal working conditions, are maintained in the relative ranges of desired values.
  • the flow rates of additional water W to nanofiltration and/or of the NFC concentrate must be suitably varied.
  • valves In order to measure and regulate all the flow rates valves are provided, with a flow measurer, or flow rate measurer, associated or for example integrated; the valves are indicated schematically in the attached drawing by the reference VFM for each stream.
  • Both the flow measurer valves VFM and the dry matter sensors DMS detect in line the relative signals of quantities measured and send them to a control unit of the electronic type, indicated by CU in the attached drawing, of the remote type or disposed near the processing plant, to which they are connected, as shown by dashes in the attached drawing.
  • the unit CU processes the signals received and, according to one or more computer programs loaded into its memory, or interfaced therewith, regulates and commands the opening and/or closing, or modulation, of the valves VFM and, in general, consequently commands and controls the whole course of the milk processing treatment which, under normal working conditions, is thus completely automated.
  • the permeate UFP has a d.m. value comprised between about 5.6% and 5.8%, substantially equal to that of the soluble dry matter of the milk M.
  • the concentrate NFC has a d.m. value comprised between about 5.6% and 5.8%, whereas the relative permeate NFP has a d.m. value comprised between about 0.3% and 0.7%.
  • the permeate NFP is recircled to ultrafiltration UF in order to dilute the stream that is actually ultra-filtered, until the permeate UFP has a d.m. value comprised in a range of desired values between about 0.3% and 3.7%, advantageously between about 1.5% and 2%.
  • the ultrafiltration retentate UFR also has a soluble d.m. value much lower than the initial starting value, comprised in a range of desired values between about 0.3% and 3.7%, advantageously between about 1.5% and 2%.
  • the total d.m. value of the diluted ultrafiltration retentate, which makes up the final product LFM, under normal working conditions is equal to said soluble d.m. value of the UFR retentate, plus the percentage of proteins and possible fats present in the original milk, which are considered insoluble and in any case remain in the stream of the ultrafiltration retentate UFR.
  • the d.m. value of the concentrate NFC increases, preferably to a range of desired values between about 8% and 30%, preferably between about 9% and 12% under normal working conditions in stationary state.
  • the d.m. value of the permeate NFP is a parameter which, in optimum conditions, must remain substantially constant in a range comprised between about 0.3% and 0.7% and is determined by the separating capacity of the nanofiltration NF membrane.
  • the d.m. value of the ultrafiltration permeate UFP settles at a determinate value, comprised in the desired range between about 1.5% and 2% and indicative of a low d.m. value of the retentate UFR, this means that the stationary state has been reached. Consequently, the streams entering M and W and emerging LFM (ultrafiltration retentate UFR diluted by the nanofiltration permeate NFP) and NFC are activated, continuously and with determinate flow rates, so as to continuously produce the milk LFM as final product and the lactose concentrate.
  • the method according to the present invention allows to reduce to a desired value the content of dry matter, and hence of lactose, of the stream of finished product LFM.
  • both ultrafiltration UF and nanofiltration NF are performed in the range of temperature allowed by the membrane processes used, for example by means of a suitable pre-heating of the milk M.
  • the range of temperature is of the usual type, and known in the state of the art, for example comprised between about 5 0 C and 50 0 C, or can also be at higher temperatures, for example about 60 0 C, 70 0 C, 80 0 C or 90 0 C, or lower, for example about O 0 C, 1°C, 2 0 C, 3°C or 4 0 C.
  • the working pressure of the ultrafiltration and nanofiltration units UF and NF is that recommended by the membrane producers, that is, a few bar, for example comprised between about 1 bar and 4 bar for ultrafiltration, and a few bar and several tens of bar, for example between about 5 bar and 40 bar for nanofiltration.
  • the ultrafiltration and nanofiltration operations can be provided in a single phase or in several cascade phases, with possible recircling of the streams, or a combination of these solutions.
  • the hydrolysis is advantageously performed before ultrafiltration UF. Subsequently, the hydrolyzed milk HM is fed normally to ultrafiltration UF and the process according to the invention proceeds, in order to reduce the glucose and galactose.
  • the enzymatic hydrolysis can be performed on the final product LFM, or on the retentate UFR, so as to reduce the content of residual lactose.
  • the milk can be subjected, as we said, to an operation to standardize the fat, block S, by means of centrifugal separation so as to separate the cream from the milk, in order to reduce the fat content and obtain skimmed or partly skimmed milk.
  • This variant is advantageous since it implies a reduced deposit of fats, the so-called fouling effect, on the membranes used in filtering.
  • a milk is obtained that has reduced calorie content both in terms of sugar and also in terms of fat.
  • This milk with low sugar content and low fat content, is suitable for consumers following a diet that provides a limited quantity of these nutrients.
  • the milk can also be subjected to heat treatment to guarantee conservation.
  • the heat treatment can be performed on the milk LFM downstream of the membrane filtering operations, as indicated by block HT.
  • a heat treatment can also be carried out before the membrane filtering operations.
  • the milk can be pasteurized, at a temperature comprised between about 60 0 C and 90 0 C, for example at about 72°C for 15 seconds, ultra- pasteurized using the ESL method for example at a temperature of about 130 0 C for about 1 - 2 seconds, or subjected to U.H.T. treatment (Ultra High Temperature) at a temperature of about 145°C for about 2 - 4 seconds, and homogenized at a pressure comprised between about 100 and 300 bar.
  • U.H.T. treatment Ultra High Temperature
  • milk with low sugar content is obtained, and optionally also with low fat content, with the desired properties of hygiene and preservation.
  • Another variant provides to apply the teachings of the international patent application WO-A-2004/110158, in the name of the present Applicant, so as to obtain milk both with a reduced sugar content and also of the ESL type, that is, long life, but which has not been subjected to too strong heat treatments or for too long a time, such as for example the U.H.T. pasteurization treatment, which could denature the nutrients originally present in the milk and worsen the original organoleptic properties.
  • the initial milk is subjected to skimming and centrifugal clarification in order to separate the fat and to kill about 70% - 90% of bacterial content and reduce the content of other microbes and pathogenic substances.
  • the milk then follows the main method according to the invention to reduce the sugars.
  • the skimmed milk with its reduced sugar content, as obtained by the steps of the method according to the main solution, is optionally subjected to heating to 50 0 C - 60 0 C, and then subjected to micro-filtering, in one or more stages, in order to obtain milk with a low bacterial and microbe content.
  • This milk is finally standardized to the desired fat content and subjected to low-temperature pasteurization. In this way, milk is obtained with a long shelf life.

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  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Food Science & Technology (AREA)
  • Polymers & Plastics (AREA)
  • Dairy Products (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Tea And Coffee (AREA)

Abstract

La présente invention concerne un procédé d'obtention de lait à faible teneur glucidique à partir de lait, comprenant au moins deux étapes : une première étape au cours de laquelle le lait est soumis à une ultrafiltration de façon à obtenir, en sortie, un perméat d'ultrafiltration et un rétentat d'ultrafiltration ; et une seconde étape au cours de laquelle le perméat d'ultrafiltration est soumis à une nanofiltration de façon à obtenir, en sortie, un perméat de nanofiltration et un concentrat de nanofiltration. Le perméat de nanofiltration est directement remis en circulation de façon continue au niveau de l'étape d'ultrafiltration de façon à diluer le rétentat d'ultrafiltration et d'obtenir le lait à faible teneur glucidique à partir de celui-ci.
PCT/EP2008/063165 2007-10-01 2008-10-01 Procédé et installations permettant d'obtenir du lait à faible teneur glucidique WO2009043882A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
CA2701066A CA2701066C (fr) 2007-10-01 2008-10-01 Procede et installations permettant d'obtenir du lait a faible teneur glucidique
AU2008306878A AU2008306878B2 (en) 2007-10-01 2008-10-01 Method and plant to obtain milk with low sugar content

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ITUD20070181 ITUD20070181A1 (it) 2007-10-01 2007-10-01 Procedimento ed impianto per ottenere latte a basso contenuto di zuccheri
ITUD2007A000181 2007-10-01

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WO2009043882A1 true WO2009043882A1 (fr) 2009-04-09

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PCT/EP2008/063165 WO2009043882A1 (fr) 2007-10-01 2008-10-01 Procédé et installations permettant d'obtenir du lait à faible teneur glucidique

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AU (1) AU2008306878B2 (fr)
CA (1) CA2701066C (fr)
IT (1) ITUD20070181A1 (fr)
WO (1) WO2009043882A1 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8445052B2 (en) 2007-10-03 2013-05-21 Arla Foods Amba Process for producing lactose-free milk
US8986768B2 (en) 2008-08-29 2015-03-24 Valio Ltd. Low-lactose and lactose-free milk product and process for production thereof
EP2907393A1 (fr) * 2014-02-17 2015-08-19 DMK Deutsches Milchkontor GmbH Produits du lait dénué du lactose
WO2016099240A1 (fr) * 2014-12-18 2016-06-23 International Business Enterprise, S. De R.L. De C.V. Procédé pour la séparation de lactose du lait pour la production de lait sans lactose et l'exploitation du sous-produit
WO2017119806A1 (fr) * 2016-01-07 2017-07-13 Comercializadora De Lácteos Y Derivados, S.A. De C.V. Procédé pour la production de lait sans lactose à haute teneur en protéines et calcium et lait sans sucre
CN112702924A (zh) * 2018-09-27 2021-04-23 利乐拉瓦尔集团及财务有限公司 橙汁的生产

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2125137A1 (en) * 1971-02-12 1972-09-29 Genvrain Sa Delactosed milk prepn - by ultra filtration of milk followed by inverse osmosis to separate lactose
DE2354475A1 (de) * 1972-11-03 1974-05-16 Azienda Municipale Della Centr Verfahren zur herstellung einer diaetmilch mit veraendertem lactosegehalt
US5503750A (en) * 1993-10-04 1996-04-02 Russo, Jr.; Lawrence J. Membrane-based process for the recovery of lactic acid by fermentation of carbohydrate substrates containing sugars
US5685990A (en) * 1992-05-04 1997-11-11 Md Foods A.M.B.A. System and a process for membrane filtration of a dispersion
FR2809595A1 (fr) * 2000-06-05 2001-12-07 B S A Derive laitier presentant une composition minerale et en acides amines selectivement modifiee, procedes pour sa fabrication, et utilisation.
WO2003094623A1 (fr) * 2002-05-14 2003-11-20 Valio Ltd Methode de production d'un produit laitier sans lactose
US20040040448A1 (en) * 2002-08-27 2004-03-04 Dunker John M. Dairy compositions and method of making
US20050196508A1 (en) * 2004-03-05 2005-09-08 Joseph Wang Lactose-removed milk product and process for the preparation thereof
US20070166447A1 (en) * 2002-08-27 2007-07-19 Select Milk Producers, Inc. Dairy compositions and method of making

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2125137A1 (en) * 1971-02-12 1972-09-29 Genvrain Sa Delactosed milk prepn - by ultra filtration of milk followed by inverse osmosis to separate lactose
DE2354475A1 (de) * 1972-11-03 1974-05-16 Azienda Municipale Della Centr Verfahren zur herstellung einer diaetmilch mit veraendertem lactosegehalt
US5685990A (en) * 1992-05-04 1997-11-11 Md Foods A.M.B.A. System and a process for membrane filtration of a dispersion
US5503750A (en) * 1993-10-04 1996-04-02 Russo, Jr.; Lawrence J. Membrane-based process for the recovery of lactic acid by fermentation of carbohydrate substrates containing sugars
FR2809595A1 (fr) * 2000-06-05 2001-12-07 B S A Derive laitier presentant une composition minerale et en acides amines selectivement modifiee, procedes pour sa fabrication, et utilisation.
WO2003094623A1 (fr) * 2002-05-14 2003-11-20 Valio Ltd Methode de production d'un produit laitier sans lactose
US20040040448A1 (en) * 2002-08-27 2004-03-04 Dunker John M. Dairy compositions and method of making
US20070166447A1 (en) * 2002-08-27 2007-07-19 Select Milk Producers, Inc. Dairy compositions and method of making
US20050196508A1 (en) * 2004-03-05 2005-09-08 Joseph Wang Lactose-removed milk product and process for the preparation thereof

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8445052B2 (en) 2007-10-03 2013-05-21 Arla Foods Amba Process for producing lactose-free milk
US8986768B2 (en) 2008-08-29 2015-03-24 Valio Ltd. Low-lactose and lactose-free milk product and process for production thereof
EP2907393A1 (fr) * 2014-02-17 2015-08-19 DMK Deutsches Milchkontor GmbH Produits du lait dénué du lactose
WO2016099240A1 (fr) * 2014-12-18 2016-06-23 International Business Enterprise, S. De R.L. De C.V. Procédé pour la séparation de lactose du lait pour la production de lait sans lactose et l'exploitation du sous-produit
WO2017119806A1 (fr) * 2016-01-07 2017-07-13 Comercializadora De Lácteos Y Derivados, S.A. De C.V. Procédé pour la production de lait sans lactose à haute teneur en protéines et calcium et lait sans sucre
CN112702924A (zh) * 2018-09-27 2021-04-23 利乐拉瓦尔集团及财务有限公司 橙汁的生产

Also Published As

Publication number Publication date
ITUD20070181A1 (it) 2009-04-02
CA2701066A1 (fr) 2009-04-09
AU2008306878A1 (en) 2009-04-09
AU2008306878B2 (en) 2014-02-20
CA2701066C (fr) 2016-11-29

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