ELECTRODIALYSIS OF FOOD PRODUCTS

Abstract: A process for modifying the acidity and ion content of an aqueous food product by electrodialysis in a system com­ prising a pair of electrodes and two or more membranes which are either exclusively cation-permeable or exclusively anion-permeable, wherein a feed stream is separated by a membrane from a waste stream, the latter containing a dilute aqueous acid solution when the membranes are cation-­ permeable and a dilute aqueous basic solution when the membranes are anion-permeable to which system the application of an electric field between the electrodes causes migration through the membranes of either protons or hydroxyl ions out of the waste stream into the feed stream and either cations or anions respectively out of the feed stream towards their respective attracting electrodes. The process is valuable for reducing the acidity of instant coffee.

Description: Elecroalsis of Food Products The present invention relates to a method for modifying the acidity and ion content of a food product by electrodialy sis. It is sometimes desirable to reduce the acidity of certain food products. For example, instant coffee with a reduced acid content is particularly suitable for people who suffer from gastric hyperacidity. Also some citrus juices have a relatively high acid content and consequently a sour taste. Normally, sugar is added to mellow the taste but sugar increases the calorie intake. If the acidity were reduced the taste would become mellow without requiring added sugar and therefore the calorie intake would not be increased. One object of this invention is to reduce the acidity of a food product without increasing the calorie content. It is also sometimes desirable to increase the acidity or reduce mineral or ash content of certain foodstuffs. For example, one of the major obstacles to the use of whey solids in human nutrition is the high mineral or ash content. Also coffee with a reduced potassium content would be desirable for malfunctioning kidney sufferers. Another object of this invention is to reduce the mineral or ash content and at the same time increase the acidity of a food product, without removing the anions. Electrodialysis is a well known process for the removal of electrolytes from a colloidal solution which basically entails applying an electric field between electrodes in pure water outside two dialysing membranes of opposite charge between which is contained the colloidal solution from which the electrolytes are to be removed. In this process the ne gatively-carged membrane is cation-permeable and the positively-charged membrane is anion-permeable: the cation-per- meable membrane allows the diffusion of cations towards the cathode but being negatively-charged it repels the anions, whereas the anion-permeable membrane allows the diffusion of anions towards the anode but being positively-charged it repels the cations. However, in this process both cations and anions are removed from the colloidal solution and the acidity therefore remains unchanged. The demineralisation of whey by electrodialysis has been described by R-.A,M, Delaney in The Australian Journal of Dairy Technology, March 1976, pp 12-14. In this process there is a series of compartments divided by alternate anion-permeable and cation-permeable membranes with streams of aqueous whey and water flowing through alternate compartments. When an electric field is applied the cations in the whey migrate towards the cathode through the cation-permeable membranes into the water streams and the anions in the whey migrate towards the anode through the anion-permeable membranes into the water streams. In this process also anions are removed-as well as cations, and the acidity remains unchanged. The processes described above require the presence of both positively-charged and negatively-charged dialysing membranes.in the system. We have found, surprisingly, that an electrodialysis process in which all the dialysing membranes in the system have the same charge can be extremely versatile in that it can be used to reduce or increase the acidity and/or reduce the mineral content of food products as desired in the following ways: a) by using membranes which are exclusively anion-permeable and substituting a dilute aqueous basic solution for the water, the acidity of the food product is reduced and b) by using membranes which are exclusively cation-permeable and substituting a dilute aqueous acidic solution for the water, the acidity of the food product is increased and the mineral content is reduced. In this invention the stream containing the aqueous food product will be referred to as the feed stream and the stream containing the dilute acid or dilute alkali will be referred to as the waste stream. The present invention provides a process for modifying the acidity and ion content of an aqueous food product by electrodialysis in a system comprising a pair of electrodes and two or more membranes which are either exclusively cation-permeable or exclusively anion-permeable, wherein a feed stream is separated by a membrane from a waste stream the latter containing a dilute aqueous acidic solution when the membranes are cation-permeable and a dilute aqueous basic solution when the membranes are anion-permeable, to which system the application of an electric field between the electrodes causes migration through the membranes of either protons or hydroxyl ions out of the waste stream into the feed stream and either cations or anions respectively out of the feed stream towards their respective attracting electrodes. For example, if there are just two membranes in the system, the feed stream m#--r flow through the compartment formed by the space between the membranes. Where there are more than two membranes in the system, both feed and waste streams may flow respectively through separate compartments formed by the spaces between adjacent membranes. In one embodiment of the process according to the present invention the acidity of a food product may be reduced when the membranes are anion-permeable and the waste stream contains a dilute aqueous basic solution, wherein the appli cation of an electric field causes migration of hydroxyl ions out of the waste stream into the feed stream and anions out of the feed stream towards the anode, for example into the waste stream. The basic solution in the waste stream may comprise any hydroxide capable of producing soluble hydroxyl ions in the system or another base, salt or oxide which is basic in aqueous solution for example potassium carbonate, sodium carbonate, potassium oxide, sodium oxide, potassium peroxide, sodium peroxide or organic bases such as methylamine, ethylamine or propylamine. Solutions of compatible mixtures of bases, basic salts or bases and basic salts may also be used. Preferably,-however the basic solution comprises a free base, especially ammonium hydroxide or an alkali- metal hydroxide such as potassium hydroxide. The concentration of the base in the waste stream depends inversely on the strength of the base used and may be from 0.05 % to 10 % preferably 0.1 % to 0.5 % on a weight/weight basis for a strong alkali metal hydroxide such as potassium hydroxide and from 1 % to 25 % preferably 2 % to 4 % on a weight/weight basis for a weaker hydroxide such as ammonlum hydroxide. In this embodiment of the invention, as the membranes are positively charged, the migration of protons and cations towards the cathode is repelled and the hydroxyl ions which have migrated out of the waste stream combine with the free hydrogen ions remaining in the feed stream to form water, thus reducing the acidity of the food product. This embodiment may be used to reduce the acidity of an extract of green or roasted coffee, a grain extract, or a tea or coffee product admixed with a grain, chocolate or chicory product. In particular, this embodiment may be used to reduce the acidity of coffee liquors which may or may not be decaf- feinated, and is especially valuable for reducing the acidity of instant coffee. The acids removed from the coffee are usually of low molecular weight for example formic, acetic, oxalic, malic and citric acids. Generally chlorogenic acid and caffeine are not removed. In another embodiment of the process according to this invention, the-mineral content of a food product may be reduced and the acidity correspondingly increased when the membranes are cation-permeable and the waste stream contains a dilute aqueous acidic solution, wherein the application of an electric field causes protons to migrate out of the waste stream into the feed stream and cations to migrate out of the feed stream towards the cathode, for example into the waste stream. The acidic solution in the waste stream may comprise a mineral or organic acid, or a salt which is acidic in aqueous solution. Examples of acids are nitric, sulphuric, hydrochloric, phosphoric, formic, acetic, citric, oxalic, malic, tartaric or ascorbic acid. Examples of salts are ammonium chloride, ammonium sulphate, monobasic and dibasic salts or citric and phosphoric acids and the monobasic salts of oxalic acid. Solutions of compatible mixtures of acids, acidic salts, or acids and acidic salts may be used. However, it is preferable to use a free acid in the waste stream. The concentration of the acid used depends inversely on its strength and when a strong acid such as phosphoric acid is used the concentration may be from 0.05 t to 10 %, preferably from 0.1 i to 0.4 % on a weight/weight basis and when a weak acid such as acetic acid is used the concentration may be from 1 % to 35 %, preferably from 2 % to 10 % on a weight/weight basis. When the food product is a coffee extract or a mixture containing a coffee extract a particularly desirable acidic solution which may be used in the waste stream is the evaporator condensate. The evaporator condensate is obtained from aqueous coffee extract, usually containing from 15 to 22 t solids, which is first stripped to remove volatile aroma components and then subjected to evaporation, usually a multistage evaporation, so that it is concentrated to a solids content of about 55 %. In the evaporation step, volatile acids that were not removed in the preceding aroma stripping are evolved, and at the same time, some non-volatiie coffee components interact and break down, giving rise to additional volatile acids which are also evolved along with water vapour. These volatile acids and water vapour thus removed from the coffee liquor are condensed into what is generally called the evaporator condensate. The main acids present in evaporator condensates are formic, acetic, propanoic, butanoic, pentanoic, 3-hexanoic, lactic, octanoic and decanoic acids. The concentration of the organic acids in the evaporator condensates is usually not more than 0.15 % titratable acids expressed as acetic acid. However, since the acids present in the evaporator condensates are derived from coffee, the use of such condensates helps to preserve the natural image of the coffee. In this embodiment, as the membranes are negatively-charged the migration of anions towards the anode is repelled. The departure of cations from the feed stream reduces the mineral content and the entry of protons increases the acidity. If reduction of the mineral content is the primary objective, the increase in acidity is a secondary result and vice versa. This embodiment may be used to reduce the mineral content of food products such as an extract of green or roasted coffee, tea, milk, whey, grain extracts and any mixture of these substances or any mixture of one or more of these substances with a fruit juice or vegetable extract. The tea extract is preferably prepared by extraction with water at a temperature of at least 750C and preferably from 800C to 1200C. Preferably acidic or basic material used in the waste stream has low cost, low toxicity, no deleterious effect on the organoleptic properties of the food, no attack on the membranes and is acceptable as a food additive. The process of this invention is generally carried out in an electrodia lysis unit several tes of which are commercially available, in which the system comprises a multiplicity of membranes forming a membrane stack wherein the feed and waste streams both flow respectively through separate ccEpartments formed by the spaces between adjacent membranes. Preferably, the feed and waste streams flow respectively through alternate canprt- ments and desirably the waste stream flows through the compartments next to each electrode car#ent. In practice, a third current conducting stream known as the electrode stream advantageously flckls through the electrode compartments of the systen. The electrode stream is either water, a dilute aqueous acidic so lution if the waste stream is acidic or a dilute aqueous basic solution if the waste stream is basic. The electrode stream may contain any of the acidic or basic materials which may be present in the waste stream and it may or may not have the same composition and/or concentration as the waste stream. The presence of the electrode stream reduces contamination of the feed by the products of the electrode reactions. Either the waste stream or the feed stream may flow through the ccmpartments adjacent to the elec trode stream. When the feed stream flows through the compartments next to the electrode stream, the latter is preferably water or a solution of a free acid or a free base. The cations or anions which migrate out of the feed stream when an electric field is applied, flow towards their respective attracting electrodes into the electrode stream. When the waste stream flows through the catn#artments next to each electrode stream, this has the effect of further minimising contamination of the feed by the products of the electrode reactions. In this case the electrode stream conveniently has the same composition as the waste stream. The flow rate of the electrode stream is not critical but should be fast enough to nep off the pockets of oxygen and hydrogen gas liberated at the electrodes. Aivant2geously, the feed and waste streams flow through their respective compartments in parallel in order to minimise electrical and mechanical resistance for either aco-current or countercurrent flow, but preferably a co-current flow. The streams may be recirculated through the system several times until the desired degree of acid modification is achieved and although the time taken is not critical, it is preferably not more then 2 hours for practical and economic reasons. The following parameters affect the rate of modification of the acidity and ion content of the food product. a) The solids content of the feed stream is preferably from 1 to 35 % by weight. Above 35 % solids content the rate decreases because the feed stream tends to form stagnant layers over the membrane surface because of its high vis cosity; b) the rate increases when the flow through the compartments becomes more turbulent. Turbulent flow not only reduces the formation of stagnant layers over the membrane sur face but also minimises the deposit of solid matter from the feed stream on the membranes, particularly coffee so lids during the acidity modification of coffee; c) within limits the rate increases with increasing flow rate. However it is not advisable to increase the flow rate beyond the maximum operating pressure recommended by the supplier of the electrodialysis unit. The flow rates of the feed and waste streams may be from 2.25 to 45.5 preferably from 7 to 23, and especially from 16 to 21 kilograms per minute; d) the rate increases with increasing temperature. However, temperatures above approximately 4000 shorten the membra ne life and generally the operating temperature is from 40C to 980C, preferably from 2400 to 650C, and optimally 3200 to 430C; e) the rate increases with increasing current up to a maxi mum and then decreases. The optimum current depends on a variety of factors such as membrane area, temperature, and resistivity of the membranes as well as of the elec trode, feed and waste streams. However, the current actually used may be somewhat above or below the optimum and expressed as current density is conveniently from 0.7 to 170 amps and preferably from 20 to 140 amps per sq. metre surface area of a single membrane. f) the rate increases with increasing concentration of the acid or hydroxide in the waste stream because increased concentration of acid or hydroxide causes greater flux of protons or hydroxyl ions through the membrane from the waste stream. However, if the acid or hydroxide con centration becomes too high, the membrane life is shor tened and increases the possibility of anion or cation leakage respectively into the feed stream; g) when other factors remain the same, the rate is directly proportional to the total surface area of the membranes in the system which in turn depends on the area of each membrane and the number of membranes in the system. Com mercially available electrodialysis units come in various sizes and contain varying numbers of membranes in the stack for example from 30 to several thousand. The sur face area of each membrane may vary within wide limits for example from 0.0232.to 0.500 square metre and the total surface area of the membrane stack may be for example from 0.2 to 500 square metres depending on the requirements; h) the rate is gradually reduced by the build up of salts in the waste stream during the process even when the acid or hydroxide concentration is maintained at its original level. Because of the great difference in the solids content of the feed stream and the waste stream, there is an osmotic flow of water from the waste stream into the feed stream. To compensate for this, a back pressure may be applied on the feed stream, for example at the point of discharge from the membranes. The back pressure is generally from 70 to 700 c per sq. cm. After each run not only does the feed stream need replenishing with fresh food product and the waste stream with acid or hydroxide but the electrode stream also requires replenishing as it becomes slightly depleted. Moreover, it is desirable to clarify the cell extract to remove suspended matter that abrades and settles on the membranes. The electrodialysis process may be carried out batchwise or continuously by conventional methods. After the acidity and ion content have been modified in accordance with this invention, the food product may subsequently be processed by conventional means. The following examples further illustrate the present in vention in which the equipment used in Examples 1 to 6 and 8 to 11 was a Mark II, 45 cm x50 cm Electrodialysis Unit by Ionics Inc. Watertown, Massachusetts. In Examples 1 to 5, 64 iS 204-UZL anion-permeable membranes and tortuous path spacers, each with a surface area of 1624 sq. cm, and having a total surface area of 10.4 sq. metres were used, and in Examples 6 to 8 to 14 34 b 61-CZL cation-permeable membranes and tortuous path spacers each with a surface area of 1624 sq. cm were used. In Example 3 a 22.5 cm x 25 cm Electrodialysis unit, also by Ionic Inc. was used in which 50 4R 61 CZL cation-permeable membranes and tortuous path spacers each with a surface area of 232 sq. cm were used. The titration of the acids and the pH measurements were carried out in the following manner. Two gram solids of the extract or powder were diluted with deionized water to give a 1 % solution which was titrated with 0.1 N NaOH on a pH meter to pH 7.0. The results are expressed as milligrams of acetic acid per gram of coffee solids. The pH was determined in a 1 % solution. Both the pH measurements and titration were carried out at room temserature. The current density is expressed as amps/ square metre of a single membrane. The percentages in the Examples are by weight. Example 1 Coffee extract containing 17.3 % solids was steam stripped to remove volatile aroma components. The stripped extract had a pH of 4.2 and contained 32.0 mg of titratable acidity as acetic acid per gram of solids before electrodialysis. A portion of the stripped extract was processed and spray dried in the conventional manner (no electrodialysis) to serve as a control. The control spray dried powder had a pH of 4.7 and contained 30.05 mg of titrable acidity as acetic acid per gram of solids. Another 100 kg of the same stripped cell extract containing 17.3 % solids was deacidified by electrodialysis under the following conditions: Operating temperature = 38 C Current = 16 amperes Current density = 107.7 amps/sq. metre Feed flow = 18.6 kg/min 200 kg of 0.3 % aqueous potassium hydroxide was placed in the waste tank and 100 kg of 0.3 % aqueous potassium hydroxide in the electrode tank. Waste flow = 18.6 kg/min Electrode flow = 7.7 kg/min The three streams were recirculated through the membrane stack for one hour. The feed stream then had a pH of 5.3 andtitratable acids equivalent to 10.8 mg acetic acid per gram solids, indicating that 66.3 % of thetitratable acids were removed. The electrodialyzed extract was processed and spray dried in the usual manner. The low acid powder had a pH of 5.3 and titratable acids equivalent to 15.2 mg acetic acid per gram solids. Compared with the control powder, the low acid powder contained 49.4 % less acids. Example 2 Coffee extract containing 14 % solids was steam stripped to remove volatile aroma components. The stripped extract had a pli of 4.6 andtitr & able acids equivalent to 24.9 mg acetic acid per gram of solids. A portion of this stripped extract was processed and spray dried in the conventional manner (no electrodialysis) to serve as a control. This control spray dried powder had a pH of 4.7 and titratable acids equivalent to 24.7 mg acetic acid per gram solids. A 200 kg batch of the same stripped extract was electrodialyzed against 0.3 % potassium hydroxide as described in Example 1. After 1. hour and 20 minutes, the extract had a pH of 6.95 and titratable acids equivalent to 0.3 mg acetic acid per gram solids, that is 98.8 % less acids than the starting extract. The low acid extract was processed and spray dried in the usual manner. The low acid powder had a pH of 6.00 and titratable acids equivalent to 6.28 mg acetic acid per gram solids. The low acid powder contained 74.6 less acids than the control powder. Example 3 An extract of decaffeinated coffee beans containing 14.7 % solids was steam stripped to remove volatile aroma components. The pH of the stripped extract was 4.75 and contained titratable acids equivalent to 24.8 mg acetic acid per gram solids. A part of this extract was spray dried without electrodialysis to serve as a control. This control powder showed a pH of 4.80 and titratable acids equivalent to 23.40 mg acetic acid per gram solids. A 200 kg batch of the stripped decaffeinated extract was deacidified by electrodialysis against 0.3 % potassium hydroxide as described in Example 1. After 1 hour and 25 minutes the extract had a pH of 6.45 and titratable acids equivalent to 4.20 mg acetic acid per gram solids, that is 83.1 % less acids than the starting extract. The low acid extract was processed and spray dried in the usual way. The low acid powder showed a pH of 6.05 and titratable acids equivalent to 6.83 mg acetic acid per gram solids, that is 70.8 % less acids than the control powder. Example 4 An extract of decaffeinated coffee beans containing 15.2 % solids was steam stripped to remove volatile aroma components. The pH of the stripped extract was 4.30 and contained titratable acids equivalent to 37.65 mg acetic acid per gram of solids. A part of this extract was spray dried without electrodialysis to serve as a control. This control powder had a pH of 4.65 and titratable acids equivalent to 26.65 mg acetic acid per gram of solids. A 200 kg batch of the stripped decaffeinated extract was electrodialyzed under the following conditions: Operating temperature = 380C Current = 12 amperes Current density = 80.75 amps/sq. metre Feed flow = 11.4 kg/min 100 kg of 2 % ammonium hydroxide was placed in each of the electrode and waste tanks. Waste flow = 11.4 kg/min Electrode flow = 7.7 kg/min The streams were recirculated through the membrane stack for 1.5 hours. The feed stream now had a pH of 5.50 and titratable acids equivalent to 12.90 mg acetic acid per gram solids, that is 65.7 % less acids than the starting extract. The electrodialyzed extract was processed in the usual manner. The low acid powder showed a pH of 5.50 and titratable acids equivalent to 13.20 mg acetic acid per gram solids, that is 50.5 - less acids than the control powder. Example 5 An extract of decaffeinated coffee beans and roasted chicory containing 7 % solids and composed of a mixture of equal parts of coffee and chicory solids was steam stripped to remove volatile aroma components. The pH of the stripped extract was 4.5 and it contained titratable acids equivalent stripped extract was spray dried in the usual manner (no electrodialysis) to serve as a control. The spray dried powder had a pH of 4.65 andtitratable acids equivalent to 18.6 mg acetic acid per gram of solids. A 157 kg batch of the same stripped extract was electrodialyzed against 0.4 % potassium hydroxide under the following conditions: Operating temperature = 380C Current = 7 amperes Current density = 47.1 amps/sq. metre Feed flow = 20 kg/min 200 kg of 0.4 % potassium hydroxide in the waste tank and 100 kg of 0.4 % potassium hydroxide in the electrode tank. Waste flow = 20 kg/min Electrode flow = 10 kg/min The streams were recirculated through the membrane stack for 1 hour and 15 minutes. The feed stream then had a pH of 5.9 and titratable acids equivalent to 6.13 mg acetic acid per gram of solids, that is 72.7 % less acids than the starting extract. The low acid extract was processed in the usual manner. The low acid powder had a pH of 5.6 and titratable acids equivalent to 7.5 mg acetic acid per gram of solids, that is- 59.7 % less acids than the control powder. Example 6 The ash content of a tea extract was reduced in the following manner. A 100 kg batch of tea extract containing 7.5 % solids, stripped beforehand to remove volatile aroma components, was electrodialyzed against 6.0 % acetic acid solution under the following conditions: Operating temperature = 380C Current = 8 amperes Current density = 53.8 amps/sq. metre Feed flow = 10 kg/min 100 kg of 6.0 % acetic acid in each of the electrode and waste tanks Waste flow = 10 kg/min Electrode flow = 3.6 kg/min The streams were recirculated through the membrane stack for two hours. The analysis of the extract before and after electrodialysis is given below: Before After Electrodialysis Electrodialysis pH of 1 % solution 5.30 4.20 Titratable acids, Equivalent to mg acetic acid/g solids 30.15 70.8 Potassium, % (dry basis) 6.35 5.63 Calcium, mg % (dry basis) 59.0 55.5 Magnesium, mg % (dry basis) 313.0 227.0 Ash, % (dry basis) 14.40 12.28 Thus after electrodialysis,titratable acids increased by 134.8 % and the ash decreased by 2.12 %. The electrodialyzed extract is processed and dried in the usual manner. Example 7 The ash content of a coffee extract was reduced and the acidity increased by electrodialysis against a 1 % aqueous citric acid solution by a batch operation under the following conditions. Fourteen kilograms of the coffee extract containing 13.4 % solids by weight were stripped to remove volatile aroma components. The stripped extract was divided into two parts. One half of the extract was electrodialyzed in a batch operation under the following conditions, while the other half served as control: Feed = 7 kg of cell extract containing l3.A g solids by weight Feed flow = 1800 ml/min Waste = 20 litres 1 % aqueous citric acid solution Waste flow = 2000 ml/min Electrode = 7.5 litres 1 % aqueous citric acid solution Electrode flow = 1100 ml/min Current density = 99.0 amps/sq. metre Temperature = 230C Time = 15 min The three streams were recirculated through the membrane stack for 15 minutes, whereafter the feed stream had a pH of 4.3 and titrable acids of 49.17 mg per gram of solids expressed as acetic acid. For the control extract (not electrodialyzed) the corresponding values were 4.8 and 29.56 respectively. The volatile aroma components were added back to the control and the electrodialyzed extracts and the two samples were freeze dried. The analysis of the control and electrodialyzed freeze dried powders is given below: Titratable Acids Equiv to pH of 1 % Acetic Moisture Solution Acid mq/g Ash Potassium Control 5.41 4.7 28.8 9.43 3.54 Electrodialyzed 5.39 4.35 41.4 8.08 2.92 Example 8 A 100 kg batch of cold water soluble tea tannins, containing 10.4 % solids was electrodialyzed against 0.3 % phosphoric acid solution under the following conditions. Feed: 100 kg cold water soluble tea tannins con taining 10.4 % solids. Waste: 100 kg 0.3 % phosphoric acid solution. The strength was periodically checked by titration and maintained at the 0.3 % level by adding concentrated phosphoric acid. Electrode: 100 kg 0.3 % phosphoric acid solution Operating temp = 380C Current = 12 amperes Current density = 80.75 amps/sq. metre Feed flow = 15 kg/min Waste flow = 17 kg/min Electrode flow = 4 kg/min The streams were recirculated through the membrane stack for four hours. The analysis of the feed stream before electro dialysis and after two and four hours, is given below: : Before After 2 hrs After 4 hrs Electro- Electro- Electro dialysis dialysis dialysis pH of 1 % solution 7.4 5.5 5.2 Titratable acids equivalent to mg acetic acid/g solids -- 22.5 30.3 Potassium, % (dry basis) 11.71 9.84 9.31 Ash, % (dry basis) 24.38 20.22 19.07 Calcium, mg% (dry basis) 139 147 146 Magnesium, mg% (dry basis) 274 274 269 Thus, after four hours of electrodialysis, the pH dropped from 7.4 to 5.2, ash from 24.38 % to 19.07 % and potassium from 11.7 % to 9.31 %. Example 9 94 kg of cell extract of coffee, previously stripped to remove volatile aroma components, containing 10.5 % solids by weight (9.9 kg total solids), having an initial pH of 4.7 and titratable acidity to pH 7 equivalent to 33.7 mg acetic acid per gram solids, was electrodialysed against an evaporator condensate under the following conditions: : Operating temperature = 380C Current = 50 amperes Current density = 300 amps/sq. metre Waste stream = 94 kg of evaporator condensate Electrode Stream = 47 kg of evaporator condensate from same source as used in waste stream Initial pH of evapora tor condensate = 3.2 Initial titratable acids in evaporator condensate = 0.14 % expressed as acetic acid Feed flow = 6.8 kg/min Waste flow = 11.3 kg/min Electrode flow = 4.3 kg/min The three streams were recirculated through the membrane stack for 1% hours, after which the coffee extract had a pH of 4.3 and titratable acids to pH 7 equivalent to 47.43 mg acetic acid per gram solids, that is a 47.4 % increase in titratable acidity. Example 10 57 kg of stripped cell extract of coffee containing 10.5 % solids by weight (5.9 kg total solids), and having an initial pH of 5.1 and titratable acids to pH 7 equivalent to 21.7 mg acetic acid per gram solids, was electrodialysed against an evaporator condensate under the following conditions: : Operating temperature = 38 C Current = 25 amperes Current density = 200 amps/sq. metre Waste stream = 150 kg of evaporator condensate Electrode stream = 113 kg of evaporator condensate from same source as that used in waste stream Initial pH of evapora tor condensate = 3.9 Initial titratable acids in evaporator condensate = 0.04 % expressed as acetic acid Feed flow = 6.8 kg/min Waste flow = 12.3 kg/min Electrode flow = 4.3 kg/min The three streams were recirculated through the membrane stack for 23 minutes after which the coffee extract had a pH of 4.2 and titratable acids to pH 7.0 equivalent to 43.4 mg acetic acid per gram solids, that is a 100 % increase in titratable acidity. Example 11 56.5kg of stripped cell extract of coffee containing 13.9 % solids by weight (7.9 kg total solids), having an initial pH of 4.6 and titratable acids to pH 7 equivalent to 47.1 mg acetic acid per gram solids, was electrodialysed against an evaporator condensate under the following conditions: : Operating temperature = 390C Current = 40 amperes Current density = 246 amps/sq. metre Waste stream = 113 kg of evaporator condensate Electrode stream = 113 kg of evaporator condensate from same source as that used in waste stream Initial pH of evapora tor concentrate = 3.6 Initial titratable acids in evaporator condensate = O.11 % expressed as acetic acid The three streams were recirculated through the membrane stack for one hour, after which the coffee extract had a pH of 4.1 and titratable acids to pH 7.0 equivalent to 64.7 mg acetic acid per gram solids, that is a 37.5 % increase in titratable acidity

Claims: Claims 1. A process for modifying the acidity and ion content of an aqueous food product by electrodialysis in a system comprising a pair of electrodes and two or more membranes which are either exclusively cation-permeable or exclusively anion-permeable, wherein a feed stream is separated by a membrane from a waste stream, the latter containing a dilute aqueous acid solution when the membranes are cation-permeable and a dilute aqueous basic solution when the membranes are anion-permeable, to which system the application of an electric field between the electrodes causes migration through. the membranes of either protons or hydroxyl ions out of the waste stream into the feed stream and either cations or anions respectively out of the feed stream towards their respective attracting electrodes. 2. A process as claimed in claim 1 for reducing the acidity of a food product in which the membranes are anion-permeable and the waste stream contains a dilute basic solution, wherein the application of an electric field causes migration of hydroxyl ions out of the waste stream into the feed stream and anions out of the feed stream towards the anode. 3. A process as claimed in claim 2 in which the hydroxide in the waste stream is ammonium hydroxide or an alkali metal hydroxide. 4. A process as claimed in claim 3 in which the hydroxide in the waste stream is potassium hydroxide. 5. A process as claimed in claim 3 or claim 4 in which the concentration of the alkali metal hydroxide in the waste stream is from 0.1 % to 0.5 % on a weight/weight basis. 6. A process as claimed in claim 3 in which the concentration of ammonium hydroxide in the waste stream is from 2.0 % to 4.0 % on a weight/weight basis. 7. A process as claimed in claim 2 in which the food product is an extract of green or roasted coffee, a grain extract or a tea or coffee product in admixture with a grain, chocolate or chicory product. 8. A process as claimed in claim 1 for reducing the mineral content or increasing the acidity of a food product in which the membranes are cation-permeable and the waste stream contains a dilute acidic solution, wherein the application of an electric field causes migration of protons out of the waste stream into the feed stream and cations out of the feed stream towards the cathode. 9. A process as claimed in claim 8 in which the dilute acid in the waste stream is phosphoric acid. 10. A process as claimed in claim 9 in which the concentration of phosphoric acid in the waste stream is from 0.1 % to 0.4 % on a weight/weight basis. 11. A process as claimed in claim 8 in which the dilute acid in the waste stream is an evaporator concentrate. 12. A process as claimed in claim 8 in which the food product is an extract of green or roasted coffee, tea, milk, whey, grain extract, and any mixture of these substances or any mixture of one or more of these substances with a fruit juice or vegetable extract. 13. A process as claimed in claim 1 in which an electrode stream flows through the electrode compartments of the system. 14. A process as claimed in claim 13 in which the electrode stream has the same composition as the waste stream. 15. A process as claimed in claim 1 in which the feed stream contains from 1 to 5 # by weight of soluble solids. 16. A process as claimed in claim 1 in which the flow through the compartments is turbulent. 17. A process as claimed in claim 1 in which the operating temperature is from 24 0C to 650C. 18. A process as claimed in claim 1 in which the current used is from 20 amps to 140 amps per square metre of a single membrane. 19. A food product with a reduced acidity whenever prepared by a process according to claim 2. 20. A food product with a reduced ash content and an increased acidity whenever prepared by a process according to claim 8.

Inventors: HUSAINI, SAEED AHMAD
Applicants: SOCIETE DES PRODUITS NESTLE S.A.
Application year: 1981
Main classification: A23F5
IPC codes: A23F3, A23F5, A23L2