CN114606349A - Beet syrup softening method - Google Patents
Beet syrup softening method Download PDFInfo
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- CN114606349A CN114606349A CN202210525570.7A CN202210525570A CN114606349A CN 114606349 A CN114606349 A CN 114606349A CN 202210525570 A CN202210525570 A CN 202210525570A CN 114606349 A CN114606349 A CN 114606349A
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- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
- C13B20/00—Purification of sugar juices
- C13B20/14—Purification of sugar juices using ion-exchange materials
- C13B20/144—Purification of sugar juices using ion-exchange materials using only cationic ion-exchange material
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J47/00—Ion-exchange processes in general; Apparatus therefor
- B01J47/02—Column or bed processes
- B01J47/022—Column or bed processes characterised by the construction of the column or container
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/50—Regeneration or reactivation of ion-exchangers; Apparatus therefor characterised by the regeneration reagents
- B01J49/53—Regeneration or reactivation of ion-exchangers; Apparatus therefor characterised by the regeneration reagents for cationic exchangers
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Abstract
The invention discloses a beet sugar dilute juice softening method, which comprises the following steps: 1) the production process comprises the following steps: the beet sugar dilute juice passes through a decalcifying ion exchange resin column to obtain softened dilute juice; 2) and (3) backwashing: carrying out backwashing on the decalcified ion exchange resin column saturated by absorbing calcium ions; 3) a regeneration procedure: regenerating the saturated decalcified ion exchange resin column absorbing calcium ions by using NaOH softened dilute juice; 4) leaching: and leaching the regenerated ion exchange resin column by using the softened dilute juice. When the softened thin juice obtained by the method for softening the beet sugar thin juice enters the subsequent working procedures of an evaporator and the like, the scaling phenomenon of the evaporator and a crystallizing sugar boiling device is reduced, the production is not stopped because the evaporator and other devices are descaled, the continuous production of the beet sugar is realized, and the labor cost is saved. Meanwhile, the service lives of the evaporator and the crystallization sugar boiling device are prolonged.
Description
Technical Field
The invention relates to the technical field of beet sugar production, in particular to a beet sugar dilute juice softening method.
Background
In the prior art, the production processes of beet sugar are mostly similar and generally comprise: obtaining sugar raw materials, seeping out sugar, cleaning sugar juice, evaporating the sugar juice, and boiling. The production method commonly adopted in beet sugar factories aiming at sugar juice cleaning is a carbonic acid cleaning method, namely, CO is introduced on the basis of adding excessive lime 2Gases, usually two liming and two CO passing2The gas, through adjusting the pH of the sugar solution, strengthens the mixing, reaction and coagulation of various colloids in the sugar juice, fine suspended colloids in the sugar juice can be flocculated into coarse precipitates, and the precipitates can further adsorb particulate matters and pigments, so that non-sugar substances are removed to the maximum extent.
However, although the excessive lime added in the sugar juice cleaning process plays a cleaning role for the sugar juice, the hardness of the sugar juice is increased, and the subsequent evaporation and boiling of the sugar juice can continuously form scales. In particular, in the case of the evaporator, the syrup, after being concentrated by evaporation, tends to form deposits in the evaporator due to the low solubility of the calcium salt, thus reducing the heat transfer coefficient, thus making the evaporated syrup less brix and increasing the steam consumption. When the deposited scale is large, the evaporator must be stopped for cleaning. Therefore, the energy consumption of the beet sugar factory is increased, the production cost is improved, the production can not be continuously and stably carried out, and the workshop extension and the intelligent workshop reconstruction are not facilitated.
Disclosure of Invention
The invention mainly solves the technical problem that the beet sugar cannot be continuously produced due to scaling of an evaporator in the production process of the beet sugar, and provides a beet sugar dilute juice softening method and a device, so that the stage of stopping production, cleaning and scaling in beet sugar production is omitted, and the real continuous production is realized.
The invention provides a beet sugar dilute juice softening method, which comprises the following steps:
1) the production process comprises the following steps: the beet sugar dilute juice passes through a decalcifying ion exchange resin column to obtain softened dilute juice;
2) and (3) backwashing: backwashing the ion exchange resin column saturated by absorbing calcium ions;
3) a regeneration process: regenerating the ion exchange resin column saturated with adsorbed calcium ions by using NaOH softened dilute juice;
4) leaching: and leaching the regenerated ion exchange resin column by using the softened dilute juice.
Regenerating ion exchange resin column with NaOH softened dilute juice, wherein sugar can be exchanged with calcium ion in the ion exchange resin column to generate calcium sucrose (C) in alkaline environment12H22O11∙ 2 CaO), and the calcium sucrose is soluble in water, so the dilute NaOH softened juice is used as a regenerant, does not generate waste liquid which is difficult to treat on the basis of ensuring the regeneration efficiency, and is environment-friendly.
Adopting NaOH softened dilute juice as a regenerant, wherein firstly, NaOH and sodium ions in the softened dilute juice can both replace calcium ions from resin; secondly, in an alkaline environment provided by NaOH, sucrose cannot be decomposed into glucose and fructose, and sucrose and calcium ions generate water-soluble calcium sucrose, so that adverse effects such as blockage on resin cannot be caused; thirdly, softened dilute juice is used as a solvent of NaOH, regenerated effluent liquid flows back to a carbon saturation front tank, and calcium ions can be discharged out of the system after precipitation is generated and filtration is carried out. The dilute juice stock solution is not diluted in the regeneration process. Compare traditional NaCl solution, NaOH solution and do not need follow-up chloride to handle as the regenerant, can not produce high salt waste water yet, can not increase evaporation cost because the thin juice stoste is diluted yet.
The beet sugar dilute juice softening method adopts a multi-unit continuous ion exchange system, and the multi-unit continuous ion exchange system comprises 10-20 ion exchange resin columns.
The softening method of beet sugar dilute juice is preceded by cleaning process, and the beet sugar dilute juice is cleaned before entering decalcification production process. Cleaning refers to the process of removing non-sugar from the beet juice. The basic cleaning method adopted by the beet sugar factory in China is a double carbonic acid method, and the cleaning process of the method mainly comprises the steps of ash adding, filling, sulfur bleaching and filtering. And after the cleaning is finished, the beet syrup enters a decalcification system for treatment.
The production process comprises the following steps: the beet sugar dilute juice is decalcified by ion exchange resin column, and the temperature of the beet sugar dilute juice in the production process is 80-100 ℃.
And (3) backwashing: and (3) backwashing the saturated ion exchange resin column absorbing the calcium ions by adopting the heat softening dilute juice at the temperature of 80-100 ℃. The backwashing temperature is lower than the above temperature, which is liable to cause the following problems: 1, the low temperature is easy to contaminate bacteria and ferment, 2, impurities are easy to precipitate and block resin, and 3, the production process temperature before backwashing is 80-100 ℃, so that backwashing is directly carried out without treatment, and the energy consumption of evaporation is reduced.
And (3) regenerating after backwashing is finished, and cooling the ion exchange resin column by adopting softened dilute juice at 30-60 ℃ before regeneration so as to reduce the temperature of the ion exchange resin column to below 70 ℃. After the resin is cooled at low temperature, a foundation is laid for subsequent regeneration, and calcium sucrose is generated at low temperature under the alkaline condition during regeneration without generating other impurities.
A regeneration process: regenerating saturated resin by using NaOH softened dilute juice, wherein the mass percent of NaOH is 2-7%.
Leaching: and (3) carrying out cold leaching on the regenerated ion exchange resin column by adopting softened dilute juice, and controlling the temperature to be 30-60 ℃.
Preheating and leaching: preheating the ion exchange resin column with the softened dilute hot juice at 80-100 deg.C, and making the preheated ion exchange resin column be used in production process.
The leaching process and the regeneration process are connected in series and are synchronous. But the preheating after the washing is asynchronous with the regeneration, and the target of only preheating and no regeneration is realized by closing the corresponding valve.
The method for softening the beet sugar dilute juice also comprises a pretreatment process, wherein after the beet sugar dilute juice enters an ion exchange resin column saturated by absorbing calcium ions, the output liquid flows back to a beet sugar dilute juice feeding tank.
Before the beet sugar dilute juice enters the production process, the beet sugar dilute juice is pretreated by a resin column which is switched from the production process and is close to saturation by exchanging calcium ions. When the decalcification treatment is carried out on a plurality of resin columns, the resin columns which are close to saturation are switched out from the production process and are used for carrying out pretreatment on the beet syrup. The pretreatment fully utilizes the residual exchange capacity of the produced resin column, so that the ion exchange resin column is utilized to the maximum extent, and the use amount of the resin is reduced in the long term. The pretreatment is not necessary, and the whole production process is still orderly carried out after the pretreatment is omitted. The difference between the two is mainly in the difference between the first investment and the running cost.
The beet sugar dilute juice softening is a continuous process, the ion exchange resin column in the production process is saturated and then switched out from the process, and then enters the next process, namely pretreatment (which can be omitted and directly enters backwashing), and the ion exchange resin column which completes backwashing, regeneration and leaching is sequentially switched to the regeneration, leaching and production processes. Even if the ion exchange resin column is almost saturated and then switched out, the ion exchange resin column in the production process can be always kept unchanged in number, because the resin column can be switched in sequence in different processes, and the beet sugar thin juice can be softened continuously.
The decalcification ion exchange resin column is Na type strong acid cation exchange resin column.
The method for softening beet sugar dilute juice adopts a multi-unit valve array ion exchange device, the production process comprises a plurality of decalcified ion exchange resin columns connected in parallel, and the volume of a single column is 1.5-3m3. In the prior artThe decalcified ion exchange resin adopts a fixed bed form, and the volume of a single column is about 30m3Typically 2 or 3 columns, the total system being charged with a total of 30-45m resin3Left and right. When the fixed bed resin is saturated in adsorption and needs backwashing regeneration, a larger flow is needed to realize backwashing of the fixed bed resin. Because the backwashing flow rate is related to the resin quantity, impurities among the resins are washed away by backwashing, and the resins can be backwashed only when the resins reach a fluidized and expanded state. The same yield of material is treated, and the resin in one column in the traditional fixed bed is about 10-20 times of the resin amount in the multi-unit column. Therefore, the required backwash flow rate is about 10 to 20 times, and the impact on the production system is large. The main reason is that there is a column shutdown during backwash and the backwash liquid required for backwash is in large quantities, thus the impact on the system is very large and large flow impacts are also likely to damage the resin. The production efficiency is not reduced by improving the past large fixed bed into the existing small parallel unit of the plurality of decalcification ion exchange resin columns, and the production process and the connection mode are greatly improved, so that the dosage of the backwashing regenerant of the small decalcification ion exchange resin columns is reduced, and the backwashing and regenerating effects are improved.
After the softened thin juice obtained by decalcification by the method for softening the beet sugar thin juice enters a subsequent evaporator and other working procedures, the scaling phenomenon of the evaporator and a crystallization sugar boiling device is reduced, the production is not stopped because the evaporator and other devices are descaled, the continuous production of the beet sugar is realized, and the labor cost is saved. Meanwhile, the service lives of the evaporator and the crystallization sugar boiling device are prolonged.
NaOH softened dilute juice is selected as a regenerant of saturated resin, so that a plurality of problems caused by regeneration of decalcified resin after saturation are solved. The regenerated resin column is washed by the dilute juice, so that additional water is saved, and the dilute juice is not diluted; compared with the existing decalcification regeneration method, the method has the advantages that the environmental protection pressure that the high-salinity wastewater is difficult to treat is avoided, and the energy consumption of subsequent evaporation concentration is greatly reduced.
Drawings
FIG. 1 is a key process diagram (with softening section) for producing beet sugar
FIG. 2 is a flow chart of the beet sugar softening process of example 1 (taking 18 columns as an example);
FIG. 3 is a process flow diagram of a rinsing process and a regeneration process in the beet sugar softening method;
FIG. 4 is a process flow diagram of a production process in a beet sugar softening process;
FIG. 5 is a front view of an ion exchange column of the present invention;
FIG. 6 is a flow chart of the beet sugar softening process of example 2 of the present invention.
Detailed Description
The technical solution of the present invention is explained in detail below.
The beet sugar juice softening method of the invention, as shown in figure 1, comprises the following steps:
1) the production process comprises the following steps: the beet sugar dilute juice passes through a Na type strong acid cation exchange resin column to obtain softened dilute juice, and most of the softened dilute juice is sent into an evaporator to be evaporated and concentrated; in this step, Ca is contained+、K+、Na+The dilute juice is fed into Na type strong acid cation exchange resin column for ion exchange to obtain softened dilute juice with Ca removed+The thin juice of (2);
2) and (3) backwashing: carrying out backwashing on the decalcified ion exchange resin column saturated by absorbing calcium ions; and the discharged material of the backwashing is returned to a second-cleaning filtering front tank, namely a second-carbon retention tank.
3) A regeneration procedure: and adding part of the softened dilute juice obtained after ion exchange into NaOH solution to form NaOH softened dilute juice, feeding the NaOH softened dilute juice into a decalcified ion exchange resin column saturated by absorbing calcium ions to regenerate the resin, and discharging the regenerated material back to a carbon pre-saturation tank, namely a cold main ash barrel.
4) Leaching: and leaching the regenerated ion exchange resin column by using the softened dilute juice, wherein the temperature is controlled to be 30-60 ℃.
5) Preheating, namely preheating the leached ion exchange resin column by using hot softened dilute juice after leaching, controlling the temperature to be 80-100 ℃, and using the preheated ion exchange column for the decalcification production of the beet syrup.
The beet sugar dilute juice softening method adopts a multi-unit continuous ion exchange system, and the multi-unit continuous ion exchange system is different from the traditional ion exchange system in that 2-3 large ion exchange resin columns are adopted, including 10-20 small ion exchange resin columns.
The structure of the ion exchange resin column used in the beet sugar dilute juice softening method is shown in figure 5, (in order to save the position and fully utilize the space, a two-link column is generally used, the two-link column is two ion exchange resin columns which are arranged up and down, the two-link column is not communicated, as shown in figure 5.) and comprises a shell 1, Na type strong acid cation exchange resin is filled in the shell 1, an upper resin inlet 2, a lower resin outlet 3, a feed inlet 4 and a discharge outlet 5 are arranged on the shell 1, a manhole 6 is arranged between the feed inlet 4 and the discharge outlet 5, a sight glass 7 is arranged above the side of the shell 1, and two resin distributors 8 are arranged at the top end and the bottom end in each resin column shell 1. The shell 1 is also provided with a reinforced channel steel 9.
The invention can fully soften the beet sugar dilute juice, is particularly applied to beet sugar softening and decalcification, can effectively avoid the formation of scale in subsequent production equipment, ensures the continuous and stable operation of a factory production line, saves energy consumption and labor cost, and ensures the automatic and efficient operation of enterprise production.
Example 1
As shown in fig. 2, the method for softening beet sugar juice of the present invention includes a production process, a backwashing process, a regeneration process, a rinsing process, and a pretreatment process. The whole softening method is composed of 18 ion exchange resin columns. The material is conveyed to a multi-column parallel resin system, and Ca in the material liquid passes through the resin layers in the resin columns2+、Mg2+With Na on the resin+After the exchange, the content of discharged CaO can be basically reduced to below 10 mg/L. The number of the resin columns can be 10-20, and is determined according to actual conditions.
The cation resin after the exchange failure also needs to be replaced and discharged for elution and regeneration, but the resin replaced by the system is only small columns one by one, the failure degree is gradually deepened, and the resin column switched each time is the deepest in failure degree, so that the utilization rate of the resin can be obviously improved.
The specific procedures of the beet sugar dilute juice softening method are as follows:
Production process (3 # -12 # resin column): as shown in figures 2 and 4, 10 resin columns are connected in parallel to run, and the cleaned beet sugar dilute juice is connected in parallel to pass through the resin layers of the 10 resin columns for ion exchange, so as to achieve the aim of decalcification, and the softened dilute juice after decalcification flows into a discharge tank and is conveyed to be evaporated. After the resin columns run for a certain time, the exchange capacity of the resin is reduced, when the discharge of a certain resin column exceeds the discharge index of the system, the resin column needs to be switched into a production process, and the resin column which is well backwashed and regenerated is switched into the production process, so that 10 resin columns are ensured to exist in the production process all the time. The specific switching mode can be switched to the No. 3 process position one by one from the No. 12 process position, and the failure degree of the resin is gradually deepened.
Pretreatment process (1 # -2 # resin column): the resin columns switched out of the production process have certain exchange activity although the discharging index exceeds the discharging index of the system, so that part of the clean beet sugar dilute juice flows out for pretreatment, enters from the upper part of the resin column at the No. 1 process position, is connected in series with the resin column at the No. 2 process position, and is discharged back to the feeding tank, thereby ensuring the full utilization of the resin exchange activity and not influencing the discharging quality index of the whole system. And the failed resin in the pretreatment process is switched out of the pretreatment process and enters the subsequent backwashing process.
Backwashing process (18 # process station): for the resin column switched from the pretreatment process, firstly, the softened dilute juice at 80-100 ℃ is used for backwashing (entering from the bottom and exiting from the upper part of the column) so that the resin is completely fluidized and eluted, and then the softened dilute juice at low temperature is used for cooling the column in a mode of entering from the bottom and exiting from the upper part of the column so that the temperature of the ion exchange resin is reduced to be below 60 ℃. The discharged material with the insoluble impurities which is washed back flows back to a second clear filtration front tank, namely a second carbon retention tank, and is filtered again in the clear juice filtration process. The backwashed resin column is switched to the regeneration process.
Regeneration step (15 # -17 # resin column): softening with low temperature NaOH as shown in FIGS. 2 and 3Regenerating the resin column with the dilute juice, introducing the NaOH softened dilute juice into the resin column, and adding Na in the regenerated liquid+Ca on the resin2+The sugar liquid obtained after exchange is rich in Ca2+And the pH value is also high, the calcium carbonate is conveyed to a carbon saturation front tank, namely a cold main ash barrel, and then the calcium carbonate is saturated to generate precipitate and is filtered, so that calcium ions can be discharged out of the system.
Leaching process (13 # -14 # resin column): as shown in fig. 2 and 3, cold leaching is carried out, cooling water and softened dilute juice enter from the upper part of No. 13, are serially washed in the forward direction to the lower part of No. 14 and then are serially washed in a regeneration area, leaching and regeneration are synchronously carried out, the regenerated dilute juice after mixing is controlled according to the flow proportion, and the NaOH content in the dilute juice is about 2-7%.
Preheating process (13 # -14 # resin column): after leaching, the leached ion exchange resin is preheated by using softened dilute juice at the temperature of 80-100 ℃, and the station of the preheating procedure is the same as that of the leaching procedure. The preheated ion exchange resin column is switched back to the production process.
The method for softening the beet syrup juice of the invention is continuous softening and achieves the following indexes:
example 2 beet syrup softening Process
This example is basically the same as example 1, but does not include a pretreatment step, i.e., a step of switching the resin column from the production step to a backwashing step. As shown in fig. 6: the method for softening the beet sugar dilute juice comprises a production process, a backwashing process, a regeneration process and a leaching process. The whole softening method is composed of 16 ion exchange resin columns. The material is conveyed to a multi-column parallel resin system, and Ca in the material liquid passes through a resin layer in the column2+、Mg2+With Na on the resin+After the exchange, the discharged CaO content can be basically reduced to below 10 mg/L.
The exchange of the failed cation resin also needs to soften the material for eluting and regenerating the cation resin, but the resin replaced by the system is only a single small column, the failure degree is gradually deepened, and the resin column switched each time has the deepest failure degree, so that the utilization rate of the resin can be obviously improved.
The specific procedures of the beet sugar dilute juice softening method are as follows:
production process (1 # -10 # resin column): the 10 resin columns are connected in parallel to run, the clean beet sugar dilute juice is connected in parallel to pass through the resin layers of the 10 resin columns for ion exchange, the aim of decalcification is achieved, and the softened dilute juice after decalcification flows into a discharge tank and is conveyed to be evaporated. After the resin columns run for a certain time, the exchange capacity of the resin columns is reduced, when the discharge of a certain resin column exceeds the discharge index of the system, the resin columns need to be switched to the production process, and the resin columns which are well backwashed and regenerated are switched to enter the production process, so that 10 resin columns are always in the production process. The specific switching mode can be switched to the No. 1 process position one by one from the No. 10 process position, and the failure degree of the resin is gradually deepened.
Backwashing step (16 # process position): the resin column switched out from the production process is firstly backwashed by using the softened dilute juice with the temperature of 80-100 ℃ (the softened dilute juice enters from the bottom and exits from the upper part of the column) so that the resin is completely fluidized and eluted, then the column is cooled by using the low-temperature softened dilute juice to enter from the bottom and exit from the upper part of the column so that the temperature of the ion exchange resin is reduced to be below 60 ℃, the discharged material with insoluble impurities which is backwashed flows back to a second-cleaning filtration front tank, namely a second-carbon retention tank, and the resin is filtered again in the clear juice filtration process. The backwashed resin column is switched to the regeneration process.
Regeneration process (13 # -15 # resin column): regenerating the resin column with the low-temperature NaOH softened dilute juice, allowing the NaOH softened dilute juice to enter the resin column, and recovering Na in the regenerated solution+Ca on the resin2+The sugar liquid obtained after exchange is rich in Ca2+And the pH value is also high, the calcium carbonate is conveyed to a carbon saturation front tank, namely a cold main ash barrel, and then is subjected to carbon saturation production, precipitation and filtration treatment, so that calcium ions can be discharged out of the system.
Leaching process (11 # -12 # resin column): and (3) performing cold leaching, wherein cooling water and softened dilute juice enter from the upper part of No. 11, are subjected to forward serial washing to the lower part of No. 12 and then are subjected to serial washing to a regeneration area, leaching and regeneration are performed synchronously, and the mixed regenerated dilute juice is controlled according to the flow proportion, wherein the content of NaOH is about 2-7%.
Preheating process (11 # -124 # resin column): after leaching, the leached ion exchange resin is preheated by using softened dilute juice at the temperature of 80-100 ℃, and the station of the preheating procedure is the same as that of the leaching procedure. The preheated ion exchange resin column is switched back to the production process.
Example 3 resin regeneration test: regeneration of saturated resins using NaCl-control NaOH-softened thin juice
The control group adopts 10% NaCl solution as resin regeneration liquid, wherein each liter of resin regeneration salt is 200g, each liter of dilute juice contains 20g of CaO, and each liter of dilute juice contains 10g of salt for removing 1g of CaO.
In the experimental group, NaOH softened dilute juice with the mass percent of 6% is used as resin regeneration liquid, 136.8g of NaOH is used for resin regeneration per liter, 20g of CaO is contained in the dilute juice per liter, and 7.1g of NaOH is consumed per 1g of CaO removed.
The comparative indexes of the beet sugar decalcification regeneration method are as follows:
example 4 comparison of conventional ion exchange resin column and inventive Small diameter ion exchange resin column
In a multi-unit continuous ion exchange system, when 16 small columns of 1.2 m diameter are used, the resin packing volume of the whole system is 28 m3About, the running linear velocity is 30 m/h, the flow of the material which can be fed is 340 m3/h。
In a conventional fixed bed, when 2 large columns with a diameter of 3.45 m are used, the resin packing volume of the whole system is still 28 m3About, the running linear velocity is 30 m/h, the flow of the material can be 280 m3/h。
In comparison, it is known that for the same resin loading, a multi-unit continuous ion exchange system can handle significantly more material.
Meanwhile, the diameter of the small column of the ion exchange resin column is small, so that backwashing and regeneration efficiency is higher, used leacheate and regeneration liquid are less, resources are saved, and production becomes more efficient.
The present invention has been described in detail, but the description is only an outline flow of the implementation of the present invention and is not to be construed as limiting the scope of the implementation of the present invention. All equivalent changes, substitutions and improvements made within the spirit and scope of the invention should be considered as being within the scope of the invention as claimed.
Claims (10)
1. A method for softening beet sugar juice is characterized by comprising the following steps:
1) the production process comprises the following steps: the beet sugar dilute juice passes through a decalcifying ion exchange resin column to obtain softened dilute juice;
2) and (3) backwashing: carrying out backwashing on the decalcified ion exchange resin column saturated by absorbing calcium ions;
3) a regeneration procedure: regenerating the saturated decalcified ion exchange resin column absorbing calcium ions by using NaOH softened dilute juice;
4) leaching: and leaching the regenerated ion exchange resin column by using the softened dilute juice.
2. The method for softening thin beet sugar juice according to claim 1, wherein the temperature of the thin beet sugar juice in the production process is 80-100 ℃.
3. The method for softening thin beet sugar juice according to claim 1, wherein the softened thin beet sugar juice at 80-100 ℃ is used to back wash the ion exchange resin column saturated with adsorbed calcium ions; after the backwashing is finished, the resin is cooled by using the softened dilute juice at the temperature of 30-60 ℃.
4. The method for softening thin beet sugar juice according to claim 1, wherein the thin beet sugar juice is regenerated by using NaOH at a temperature of 30-60 ℃, wherein the NaOH is 2-7% by weight.
5. The beet sugar dilute juice softening method according to claim 1, wherein the regenerated ion exchange resin column is rinsed with the softened dilute juice of 30-60 ℃, and after rinsing, the ion exchange resin column is preheated and rinsed with the softened dilute juice of 80-100 ℃.
6. The beet sugar dilute juice softening method according to claim 5, wherein the ion exchange resin column in the rinsing step is connected in series with the ion exchange resin column in the regenerating step, and the softened dilute juice at 30-60 ℃ enters the ion exchange resin column in the rinsing step, and the effluent is mixed with NaOH solution and then enters the ion exchange resin column in the regenerating step.
7. The method for softening thin beet sugar juice according to claim 1, wherein in the production process, the thin beet sugar juice is softened by passing through a plurality of decalcified ion exchange resin columns connected in parallel.
8. The method for softening thin beet sugar juice according to claim 1, wherein the softening of thin beet sugar juice is a continuous process, the ion exchange resin column in the production process is saturated and then switched to a backwashing process, and the ion exchange resin column after the backwashing, regeneration and rinsing processes is switched to the production process.
9. The method for softening the dilute beet sugar juice according to claim 1, wherein the decalcifying ion exchange resin column is a Na-type strong acid cation exchange resin column.
10. The method for softening thin beet sugar juice according to claim 1, wherein the method further comprises a pretreatment step, wherein the thin beet sugar juice enters an ion exchange resin column saturated with adsorbed calcium ions, and then the effluent is returned to the thin beet sugar juice feed tank.
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| US4353992A (en) * | 1979-12-28 | 1982-10-12 | Akzona Incorporated | Process for the regeneration of a sorbent |
| CN102319592A (en) * | 2011-05-27 | 2012-01-18 | 华南理工大学 | Method for preparing inorganic potassium salt based on sugar making diethyl ether and dilute juice desalination |
| CN106669867A (en) * | 2017-03-21 | 2017-05-17 | 南京凯通粮食生化研究设计有限公司 | Continuous and automatic ion exchange device |
| CN112795710A (en) * | 2020-12-08 | 2021-05-14 | 武汉美味源生物工程有限公司 | Regeneration method of ion exchange resin in sugar production process |
-
2021
- 2021-10-22 CN CN202111235836.6A patent/CN114277197A/en active Pending
-
2022
- 2022-05-16 CN CN202210525570.7A patent/CN114606349A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4353992A (en) * | 1979-12-28 | 1982-10-12 | Akzona Incorporated | Process for the regeneration of a sorbent |
| CN102319592A (en) * | 2011-05-27 | 2012-01-18 | 华南理工大学 | Method for preparing inorganic potassium salt based on sugar making diethyl ether and dilute juice desalination |
| CN106669867A (en) * | 2017-03-21 | 2017-05-17 | 南京凯通粮食生化研究设计有限公司 | Continuous and automatic ion exchange device |
| CN112795710A (en) * | 2020-12-08 | 2021-05-14 | 武汉美味源生物工程有限公司 | Regeneration method of ion exchange resin in sugar production process |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115595383A (en) * | 2022-08-31 | 2023-01-13 | 新疆冠农果茸股份有限公司（Cn） | Process for decalcifying syrup thin juice |
| CN115595383B (en) * | 2022-08-31 | 2024-07-26 | 新疆冠农股份有限公司 | Syrup dilute juice decalcification process |
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| Publication number | Publication date |
|---|---|
| CN114277197A (en) | 2022-04-05 |
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