US3887391A - Process for the decalcification sugar beet juice - Google Patents
Process for the decalcification sugar beet juice Download PDFInfo
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- US3887391A US3887391A US443612A US44361274A US3887391A US 3887391 A US3887391 A US 3887391A US 443612 A US443612 A US 443612A US 44361274 A US44361274 A US 44361274A US 3887391 A US3887391 A US 3887391A
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- juice
- magnesium oxide
- cation exchanger
- sugar beet
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- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
- C13B20/00—Purification of sugar juices
- C13B20/02—Purification of sugar juices using alkaline earth metal compounds
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
- C13B20/00—Purification of sugar juices
- C13B20/14—Purification of sugar juices using ion-exchange materials
- C13B20/144—Purification of sugar juices using ion-exchange materials using only cationic ion-exchange material
Definitions
- Additives such as soda ash are commonly used to displace the calcium ion and to cause its precipitation as calcium carbonate according to Formula 1:
- second carbonation juice is percolated through the hydrogen form of a weak cation exchanger at a relatively high flowrate of from about 20 to about 200 bedvolumes per hour and at temperatures as high as 95 C.
- the contact time for the syrup should not exceed 3 minutes, but should preferably be held below 1 minute to minimize sucrose loss through heterogeneous inversion.
- This treatment removes most of the calcium, and also some potassium and sodium, from the second carbonation juice in exchange for hydrogen ions.
- An represents juice anions.
- sucrose extractioninhibiting cations such as sodium and potassium which are naturally occurring in the sugar beet.
- EXAMPLE 1 A sugar beet juice having been defecated via lime and CO treatment followed by a second carbonation being carbonated to minimum calcium ion concentration in the usual manner and with a pH range of 7.5-9.5 and at a temperature between -95 C., being free of suspended and precipitated solids, is treated with a weak cation exchanger having carboxylic acid functionality.
- a contact time of between 20 seconds and 3 minutes depending upon the temperature of the juice is usually sufficient to reduce the calcium ion concentration in the juice to desirable levels without significant losses of sucrose through heterogeneous inversion. That is to say, at the high temperature of C. a contact time of less than 1 minute is sufficient and desirable, while at temperatures below 70 C., a contact time of up to three minutes may be required.
- the contact time may also be lowered or extended depending upon the extent of the cation exchange desired.
- increasing the contact time will increase the cation exchange.
- the treatment of the sugar beet juice with the weak cation exchanger may proceed by percolating the juice through a compressed column of the exchanger with a bed depth for the exchanger of between 12-50 inches. Excessive pressure drops prohibit a higher bed depth, because of the extensive resin expansion which occurs while the resin converts from the hydrogen form.
- the effluent juice from the ion exchange treatment may exhibit a pH value of between 3.0 8.5 pH depending upon the original limesalt level, original alkalinity, temperature, flowrate and degree of resin exhaustion.
- the single figure of drawing illustrates a typical pH curve for such ion exchange treatment.
- Magnesium oxide is added to the juice so treated by ion exchange to obtain a final juice pH of between 8.0 9.0. Magnesium oxide addition is controlled according to the desired final pH allowing a retention time of between to minutes for dissolving required magnesium oxide and pH equilibration.
- a filtration step is usually desired after the magnesium oxide treatment to remove excess reagent and other impurities before proceeding with the evaporation and crystallization.
- the acidic functionality of the carboxylic type cation exchanger is usually exhausted after utilizing between 50-90% of its total exchange capacity.
- the degree of resin utilization is primarily dependent upon pH and alkalinity of the juice to be treated and to a lesser degree upon the contact time and operating temperature.
- Regeneration of the exhausted ion exchange resin is then achieved through contact with a suitable strong mineral acid preferably hydrochloric acid in the conventional well-established manner.
- a second carbonation juice with a brix of l4Bx containing 0.300 g CaO per 100 g dissolved dry substance and having a total alkalinity of 0.028 (expressed as grams of CaO equivalent per 100 ml solution) is passed through a 36 inch column of a weak cation exchanger having carboxylic acid functionality.
- a flowrate of 80 resin bedvolumes per hour is maintained at 85 until 300 bedvolumes of juice have passed through the ion exchange column.
- Calcium ion concentration in the treated juice will average less than 0.03 grams of CaO equivalent per 100 grams of dissolved dry substance.
- Example ll The conditions observed are the same as those outlined under Example I above except that the cation exchanger with carboxylic acid functionality is added continuously to a stream of the second carbonation juice, in the ratio of between 1/100 to 1/1000 depending on the variable as outlined.
- a simple strainer or screen is used to achieve separation of the juice from the resin particles after the appropriate contact time.
- EXAMPLE lll Conditions in this example are the same as under Examples l or II above except that after the ion exchange treatment the juice is forced through a ⁇ ertical column of granular magnesium oxide to realkalize the juice. The juice is allowed by this treatment to equilibrate to steady state which is a final pH of about 8.8.
- a process which comprises the steps of (a) treating sugar beet juice, after second carbonation, with the hydrogen form of a resinous carboxylic type cation exchanger arranged in a column for the reduction of calcium ion in the juice, at a flowrate of between 20 and 200 resin bedvolumes per hour and at a temperature of 95 C and for a contact time of between 20 seconds and 3 minutes; (b) realkalizing the so-treated juice with magnesium oxide to a pH between 7.5 and 9.5 and thereafter (c) filtering the realkalized juice to remove excess magnesium oxide and insoluble impurities.
- a continuous process which comprises the steps of treating a stream of sugar beet juice, after its second carbonation, with the hydrogen form of a resinous carboxylic type cation exchanger in a ratio required to maintain a pre-determined exchange rate in the ratio of from l/l00 to H000 and at a temperature of 7095 C. and for a contact time of between 20 seconds and 3 minutes; separating the so-treated juice from the cation exchanger, re-alkalyzing the so-treated juice with magnesium oxide to a pH between 7.5 and 9.5; and thereafter filtering the re-alkalized juice to remove excess magnesium oxide and insoluble impurities.
- a process which comprises the steps of (a) treating sugar beetjuice, after second carbonation, with the hydrogen form of a resinous carboxylic type cation exchanger arranged in a column for the reduction of calcium ion in the juice, at a flow rate of between 20 and 200 resin bedvolumes per hour and at a temperature of 7095 C and for a contact time of between 20 seconds and three minutes; (b) re-alkalizing the so-treated juice with magnesium oxide to a pH of about 8.5; and thereafter (c) filtering the re-alkalized juice to remove excess magnesium oxide and insoluble impurities.
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Abstract
Undesirable cations are removed from sugar juice which has undergone a two-stage carbonation by treating the same with the hydrogen form of a carboxylic type cation exchanger, in a column, at a flowrate of 20-200 resin bedvolumes per hour, at an elevated temperature short of boiling, for a contact time less than 3 minutes, and thereafter realkalizing with magnesium oxide and filtering.
Description
atent [1 1 tlnite States Schoenrock et al.
[ June 3,1975
[ PROCESS FOR THE DECALCIFICATION SUGAR BEET JUICE [75] Inventors: Karlheinz W. R. Schoenrock;
Preston Richey; Hugh G. Rounds, all of Ogden, Utah [73] Assignee: The Amalgamated Sugar Company,
Ogden, Utah [22] Filed: Feb. 19, 1974 [21] Appl. No.: 443,612
[52] US. Cl 127/46 A; 127/50; 127/55 [51] Int. Cl. C13d 3/02; Cl3d 3/14 [58] Field of Search 127/46 R, 46 A, 50, 48,
[56] References Cited UNITED STATES PATENTS 1/1963 Popper 127/50 X 12/1973 Nishijima 127/50 X OTHER PUBLICATIONS Sugar Industry Abstracts, Vol. 27, abstract 975 Sugar Industry Abstracts, Vol. 30, abstract 689 (1968).
Chemical Abstracts, 69:68438d (1968).
Beet-Sugar Tech., R. A McGinnis, ed. 2nd Edition, 330333, Beet Sugar Development Foundation, 1971.
Primary Examiner-Morris O. Wolk Assistant Examiner-Sidney Marantz Attorney, Agent, or FirmPierce, Scheffler & Parker [57] ABSTRACT Undesirable cations are removed from sugar juice which has undergone a two-stage carbonation by treating the same with the hydrogen form of a carboxylic type cation exchanger, in a column, at a flowrate of 20-200 resin bedvolumes per hour, at an elevated temperature short of boiling, for a contact time less than 3 minutes, and thereafter realkalizing with magnesium oxide and filtering.
5 Claims, 1 Drawing Figure Correlation Between Throughput and Effluent pH for the Treatment of Clarified Sugarbcet Juice by Weak Cation E Seconds, Temperature anger with Carhoxy ic Acid Functionality-Contact Time 20 100 Bedvolumes throughput 200 300 PROCESS FOR THE DECALCIFICATION SUGAR BEET JUICE This invention relates to the sugar refining art, and is concerned with a process of removing undesirable cationic impurities from sugar beet juice via ion exchange for cations which enhance operation, crystallization and extraction of sugar from sugar beet juice so treated.
In the conventional process the so-called first carbonation of the sugar beet juice with ensuing separation of the clear liquid from precipitated and suspended solids is followed by a second carbonation of the clear liquid. This two-stage carbonation is necessary to maximize impurity removal while minimizing the calcium ion concentration prior to the evaporation step. Under normal conditions, however, the calcium ion concentration is still excessive after this second carbonation, leading to fouling and scaling of the evaporator heating surfaces. Such fouling and scaling brings about inefficiency in heat transfer and reduction in equipment capacity.
Additives such as soda ash are commonly used to displace the calcium ion and to cause its precipitation as calcium carbonate according to Formula 1:
Ca. An Nazcog Ca CO3 Nag An where An signifies anionic impurities in the sugar beet juice.
Other so-called softening techniques which use a strong, sulfonic type cation exchanger operated over the sodium form have also found widespread application in reducing the calcium ion concentration in sugar beet juice prior to evaporation.
It is now an established fact that the sodium ion which is commonly used to displace the calcium ion either in the form of an additive or through ion exchange techniques imparts increasing solubility upon the sucrose hence reduces extraction.
In contrast to the solubility-increasing effect of sodium ions upon sucrose is the salting out or solubilitydecreasing effect of magnesium ions upon sucrose in aqueous solutions.
A process has now been discovered which allows the elimination of the scale-forming calcium ions without the introduction of molasses-forming sodium ions.
In accordance with this invention, second carbonation juice is percolated through the hydrogen form of a weak cation exchanger at a relatively high flowrate of from about 20 to about 200 bedvolumes per hour and at temperatures as high as 95 C. The contact time for the syrup should not exceed 3 minutes, but should preferably be held below 1 minute to minimize sucrose loss through heterogeneous inversion. This treatment removes most of the calcium, and also some potassium and sodium, from the second carbonation juice in exchange for hydrogen ions.
Formulas II and VI relate the chemical reactions occurring:
R(COOH) Ca An R(COO) Ca H An R(COOH) K An R(COO)K H An Ill R(COOH) Na An R(COO)Na H An R(COOK) Ca An R(COO) CA K An R(COONa) Ca An R(COO) Ca Na An where R signifies the resin matrix, and
An represents juice anions.
As can be seen from reactions In and IV, this process may also be used to reduce sucrose extractioninhibiting cations such as sodium and potassium which are naturally occurring in the sugar beet.
The occurrence of free acid in the sugar beet juice so treated may cause this juice to become undesirably acidic. A cation selected from the alkaline earth metal group but preferably magnesium oxide is added to a juice so treated to neutralize these free acids in the juice and to restore a pH which is desirable for further treatment through evaporation and crystallization. Formula VII illustrates this reaction:
H An l- MgO MgAn H O VII After exhaustion of the weak cation exchanger with calcium ions and sugar beet juice cations the resin is regenerated with a suitable acid.
Weak cation exchanger with carboxylic acid functionality such as are described by Ilelferich in Ion Exchange McGraw-Hill Book Co., 1962, pages 30-31 and commercially available under the tradenames of Amberlite RC-50; Amberlite IRC-84; Duolite CC3; Dowex CCR-l; and Lewatit CNP, among others, are suitable for this application. The named exchangers were used in the following specific examples.
EXAMPLE 1 A sugar beet juice having been defecated via lime and CO treatment followed by a second carbonation being carbonated to minimum calcium ion concentration in the usual manner and with a pH range of 7.5-9.5 and at a temperature between -95 C., being free of suspended and precipitated solids, is treated with a weak cation exchanger having carboxylic acid functionality. A contact time of between 20 seconds and 3 minutes depending upon the temperature of the juice is usually sufficient to reduce the calcium ion concentration in the juice to desirable levels without significant losses of sucrose through heterogeneous inversion. That is to say, at the high temperature of C. a contact time of less than 1 minute is sufficient and desirable, while at temperatures below 70 C., a contact time of up to three minutes may be required. The contact time may also be lowered or extended depending upon the extent of the cation exchange desired. Thus, increasing the contact time will increase the cation exchange. The treatment of the sugar beet juice with the weak cation exchanger may proceed by percolating the juice through a compressed column of the exchanger with a bed depth for the exchanger of between 12-50 inches. Excessive pressure drops prohibit a higher bed depth, because of the extensive resin expansion which occurs while the resin converts from the hydrogen form.
The effluent juice from the ion exchange treatment may exhibit a pH value of between 3.0 8.5 pH depending upon the original limesalt level, original alkalinity, temperature, flowrate and degree of resin exhaustion. The single figure of drawing illustrates a typical pH curve for such ion exchange treatment.
Magnesium oxide is added to the juice so treated by ion exchange to obtain a final juice pH of between 8.0 9.0. Magnesium oxide addition is controlled according to the desired final pH allowing a retention time of between to minutes for dissolving required magnesium oxide and pH equilibration.
A filtration step is usually desired after the magnesium oxide treatment to remove excess reagent and other impurities before proceeding with the evaporation and crystallization.
The acidic functionality of the carboxylic type cation exchanger is usually exhausted after utilizing between 50-90% of its total exchange capacity. The degree of resin utilization is primarily dependent upon pH and alkalinity of the juice to be treated and to a lesser degree upon the contact time and operating temperature.
Regeneration of the exhausted ion exchange resin is then achieved through contact with a suitable strong mineral acid preferably hydrochloric acid in the conventional well-established manner. Hence, a second carbonation juice with a brix of l4Bx containing 0.300 g CaO per 100 g dissolved dry substance and having a total alkalinity of 0.028 (expressed as grams of CaO equivalent per 100 ml solution) is passed through a 36 inch column of a weak cation exchanger having carboxylic acid functionality. A flowrate of 80 resin bedvolumes per hour is maintained at 85 until 300 bedvolumes of juice have passed through the ion exchange column. Calcium ion concentration in the treated juice will average less than 0.03 grams of CaO equivalent per 100 grams of dissolved dry substance. It requires less than one pound of magnesium oxide per 100 cu. ft. of juice treated to restore juice alkalinity to the desirable 0.023 gram CaO equivalent per 100 m1 juice and a pH of about 8.5. To regenerate the exhausted ion exchanger requires about 30 gallons of 4% HCl per cu. ft. of resin used.
Example ll The conditions observed are the same as those outlined under Example I above except that the cation exchanger with carboxylic acid functionality is added continuously to a stream of the second carbonation juice, in the ratio of between 1/100 to 1/1000 depending on the variable as outlined. A simple strainer or screen is used to achieve separation of the juice from the resin particles after the appropriate contact time.
EXAMPLE lll Conditions in this example are the same as under Examples l or II above except that after the ion exchange treatment the juice is forced through a \ertical column of granular magnesium oxide to realkalize the juice. The juice is allowed by this treatment to equilibrate to steady state which is a final pH of about 8.8.
We claim:
1. A process which comprises the steps of (a) treating sugar beet juice, after second carbonation, with the hydrogen form of a resinous carboxylic type cation exchanger arranged in a column for the reduction of calcium ion in the juice, at a flowrate of between 20 and 200 resin bedvolumes per hour and at a temperature of 95 C and for a contact time of between 20 seconds and 3 minutes; (b) realkalizing the so-treated juice with magnesium oxide to a pH between 7.5 and 9.5 and thereafter (c) filtering the realkalized juice to remove excess magnesium oxide and insoluble impurities.
2. A process according to claim 1, wherein a portion of the insoluble separated in 1(c) is recycled for realkalization.
3. A process according to claim 1, wherein realkalization is accomplished by forcing the ion exchangetreated juice through a column of granular magnesium oxide to a steady state point of alkalinity.
4. A continuous process which comprises the steps of treating a stream of sugar beet juice, after its second carbonation, with the hydrogen form of a resinous carboxylic type cation exchanger in a ratio required to maintain a pre-determined exchange rate in the ratio of from l/l00 to H000 and at a temperature of 7095 C. and for a contact time of between 20 seconds and 3 minutes; separating the so-treated juice from the cation exchanger, re-alkalyzing the so-treated juice with magnesium oxide to a pH between 7.5 and 9.5; and thereafter filtering the re-alkalized juice to remove excess magnesium oxide and insoluble impurities.
5. A process which comprises the steps of (a) treating sugar beetjuice, after second carbonation, with the hydrogen form of a resinous carboxylic type cation exchanger arranged in a column for the reduction of calcium ion in the juice, at a flow rate of between 20 and 200 resin bedvolumes per hour and at a temperature of 7095 C and for a contact time of between 20 seconds and three minutes; (b) re-alkalizing the so-treated juice with magnesium oxide to a pH of about 8.5; and thereafter (c) filtering the re-alkalized juice to remove excess magnesium oxide and insoluble impurities.
UNTTED STATES PATENT OFFICE QENMQATE 0F CORECTIQN PATENT NO. 3, 887,391
DATED Jun 3 9 7 iNVENTORiS) KARLHEINZ W .RQSCHOENROCK et a1 It is certified that error appears in the above-identified patent and that said Letters Patent are hereby corrected as shown below;
In the Title of Invention:
Before "SUGAR" Insert: OF
In claim t: line 6 "1/000" should read: l/lOOO fif Day 0 August1975 [SEAL] AIIESI.
RUTH C. MASON C. MARSHALL DANN Arresting Officer ('ummi'xsimwr of Parents and Trademarks
Claims (5)
1. A PROCESS WHICH COMPRISES THE STEPS OF (A) TREATING SUGAR BEET JUICE, AFTER SECOND CARBONATION, WITH THE HYDROGEN FORM OF A RESINOUS CARBOXYLIC TYPE CATION EXCHANGER ARRANGED IN A COLUMN FOR THE REDUCTION OF CALCIUM ION IN THE JUICE, AT A FLOWATE OF BETWEEN 20 AND 200 RESIN BEDVOLUMES PER HOUR AND AT A TEMPERATURE OF 70*-95*C AND FOR A CONTACT TIME OF BETWEEN 20 SECONDS AND 3 MINUTES; (B) REALKALIZING THE SOTR 9.5 AND THEREAFTER (C) FILTERING THE REALKALIZED JUICE TO REMOVE EXCESS MAGNESIUM OXIDE AND INSOLUBLE IMPURITIES.
1. A process which comprises the steps of (a) treating sugar beet juice, after second carbonation, with the hydrogen form of a resinous carboxylic type cation exchanger arranged in a column for the reduction of calcium ion in the juice, at a flowrate of between 20 and 200 resin bedvolumes per hour and at a temperature of 70*-95* C and for a contact time of between 20 seconds and 3 minutes; (b) realkalizing the so-treated juice with magnesium oxide to a pH between 7.5 and 9.5 and thereafter (c) filtering the realkalized juice to remove excess magnesium oxide and insoluble impurities.
2. A process according to claim 1, wherein a portion of the insoluble separated in 1(c) is recycled for realkalization.
3. A process according to claim 1, wherein realkalization is accomplished by forcing the ion exchangetreated juice through a column of granular magnesium oxide to a steady state point of alkalinity.
4. A continuous process which comprises the steps of treating a stream of sugar beet juice, after its second carbonation, with the hydrogen form of a resinous carboxylic type cation exchanger in a ratio required to maintain a pre-determined exchange rate in the ratio of from 1/100 to 1/000 and at a temperature of 70*-95* C. and for a contact time of between 20 seconds and 3 minutes; separating the so-treated juice from the cation exchanger, re-alkalyzing the so-treated juice with magnesium oxide to a pH between 7.5 and 9.5; and thereafter filtering the re-alkalized juice to remove excess magnesium oxide and insoluble impurities.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US443612A US3887391A (en) | 1974-02-19 | 1974-02-19 | Process for the decalcification sugar beet juice |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US443612A US3887391A (en) | 1974-02-19 | 1974-02-19 | Process for the decalcification sugar beet juice |
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| Publication Number | Publication Date |
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| US3887391A true US3887391A (en) | 1975-06-03 |
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| US443612A Expired - Lifetime US3887391A (en) | 1974-02-19 | 1974-02-19 | Process for the decalcification sugar beet juice |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3973986A (en) * | 1975-03-26 | 1976-08-10 | The Amalgamated Sugar Company | Process for the purification of sugarbeet juice and increasing the extraction of sugar therefrom |
| US3982956A (en) * | 1975-09-26 | 1976-09-28 | The Amalgamated Sugar Company | Process for the purification of impure sugar juice |
| US4045242A (en) * | 1976-08-17 | 1977-08-30 | The Amalgamated Sugar Company | Process for the purification of sugarbeet juice and the reduction of lime salts therein |
| FR2457897A1 (en) * | 1979-05-30 | 1980-12-26 | Generale Sucriere Sa | Treating impure sugar soln. to improve crystallisation - by ion exchange to acid form and neutralising with alkali such as magnesia |
| US4705637A (en) * | 1984-06-15 | 1987-11-10 | Bayer Aktiengesellschaft | Process for reducing the wash water requirement of weakly basic anion exchangers |
| EP0262711A1 (en) * | 1986-09-12 | 1988-04-06 | Coöperatieve Vereniging Suiker Unie U.A. | Method for demineralizing beet sugar thin juice |
| US5454875A (en) * | 1994-07-01 | 1995-10-03 | Board Of Supervisors Of Louisiana State University And Agricultural And Mechanical College | Softening and purification of molasses or syrup |
| US6238486B1 (en) | 1999-03-10 | 2001-05-29 | Nalco Chemical Company | Detectable cationic flocculant and method of using same in industrial food processes |
| US20090056707A1 (en) * | 2007-08-30 | 2009-03-05 | Iogen Energy Corporation | Process of removing calcium and obtaining sulfate salts from an aqueous sugar solution |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3073725A (en) * | 1960-12-01 | 1963-01-15 | Popper Karel | Ion exchange processes |
| US3781174A (en) * | 1970-10-16 | 1973-12-25 | Hitachi Shipbuilding Eng Co | Continuous process for producing refined sugar |
-
1974
- 1974-02-19 US US443612A patent/US3887391A/en not_active Expired - Lifetime
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3073725A (en) * | 1960-12-01 | 1963-01-15 | Popper Karel | Ion exchange processes |
| US3781174A (en) * | 1970-10-16 | 1973-12-25 | Hitachi Shipbuilding Eng Co | Continuous process for producing refined sugar |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3973986A (en) * | 1975-03-26 | 1976-08-10 | The Amalgamated Sugar Company | Process for the purification of sugarbeet juice and increasing the extraction of sugar therefrom |
| US3982956A (en) * | 1975-09-26 | 1976-09-28 | The Amalgamated Sugar Company | Process for the purification of impure sugar juice |
| US4045242A (en) * | 1976-08-17 | 1977-08-30 | The Amalgamated Sugar Company | Process for the purification of sugarbeet juice and the reduction of lime salts therein |
| FR2457897A1 (en) * | 1979-05-30 | 1980-12-26 | Generale Sucriere Sa | Treating impure sugar soln. to improve crystallisation - by ion exchange to acid form and neutralising with alkali such as magnesia |
| US4705637A (en) * | 1984-06-15 | 1987-11-10 | Bayer Aktiengesellschaft | Process for reducing the wash water requirement of weakly basic anion exchangers |
| EP0262711A1 (en) * | 1986-09-12 | 1988-04-06 | Coöperatieve Vereniging Suiker Unie U.A. | Method for demineralizing beet sugar thin juice |
| US4799965A (en) * | 1986-09-12 | 1989-01-24 | Cooperatieve Vereniging Suiker Unie U.A. | Method for demineralizing beet sugar thin juice |
| US5454875A (en) * | 1994-07-01 | 1995-10-03 | Board Of Supervisors Of Louisiana State University And Agricultural And Mechanical College | Softening and purification of molasses or syrup |
| US6238486B1 (en) | 1999-03-10 | 2001-05-29 | Nalco Chemical Company | Detectable cationic flocculant and method of using same in industrial food processes |
| US20090056707A1 (en) * | 2007-08-30 | 2009-03-05 | Iogen Energy Corporation | Process of removing calcium and obtaining sulfate salts from an aqueous sugar solution |
| US8273181B2 (en) * | 2007-08-30 | 2012-09-25 | Iogen Energy Corporation | Process of removing calcium and obtaining sulfate salts from an aqueous sugar solution |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| AS | Assignment |
Owner name: AMALGAMATED RESEARCH, INC., IDAHO Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:AMALGAMATED SUGAR COMPANY, THE;REEL/FRAME:008342/0161 Effective date: 19961224 |