CN114277196A - Beet sugar decalcification system - Google Patents
Beet sugar decalcification system Download PDFInfo
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- CN114277196A CN114277196A CN202111235828.1A CN202111235828A CN114277196A CN 114277196 A CN114277196 A CN 114277196A CN 202111235828 A CN202111235828 A CN 202111235828A CN 114277196 A CN114277196 A CN 114277196A
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- ion exchange
- exchange resin
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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
本发明公开了一种甜菜糖脱钙系统，包括：生产区包括多根并联设置的离子交换树脂柱；冷却反洗区包括从生产区切换来的失效离子交换树脂柱；再生区包括从冷却反洗区切换来的离子交换树脂柱，NaOH软化稀汁对反洗完成的离子交换树脂柱中的树脂进行再生；淋洗和预热区包括从再生区切换来的离子交换树脂柱，软化稀汁对离子交换树脂柱中的树脂进行淋洗和预热。通过本发明的甜菜糖稀汁软化方法获得的软化稀汁进入后续蒸发器等工序后，减少了蒸发器、结晶煮糖设备的结垢现象，不再因为要对蒸发器等设备进行除垢而停止生产，实现了甜菜糖的连续生产，节省人工费用。同时也延长了蒸发器和结晶煮糖设备的使用寿命。
The invention discloses a beet sugar decalcification system, comprising: a production area includes a plurality of ion exchange resin columns arranged in parallel; a cooling and backwashing area includes a failed ion exchange resin column switched from the production area; The ion exchange resin column switched from the washing zone, NaOH softens the thin juice to regenerate the resin in the ion exchange resin column after backwashing; the rinsing and preheating zone includes the ion exchange resin column switched from the regeneration zone to soften the thin juice Rinse and preheat the resin in the ion exchange resin column. After the softened thin juice obtained by the beet sugar thin juice softening method of the present invention enters the subsequent evaporator and other processes, the scaling phenomenon of the evaporator and the crystallization sugar boiling equipment is reduced, and the equipment is no longer stopped because the evaporator and other equipment need to be descaled. It realizes the continuous production of beet sugar and saves labor costs. At the same time, it also prolongs the service life of evaporator and crystallized sugar cooking equipment.
Description
Technical Field
The invention relates to the technical field of beet sugar production, in particular to a beet sugar decalcification system.
Background
The ion exchange method begins in the fortieth of the twentieth century, and has wide application in the material purification technology by utilizing the unique ion exchange performance of synthetic resin. At the end of the twentieth century, sugar producing countries from sugar beets in the world, particularly countries in Europe and America, have had a great deal of development from research to application in ion exchange for purifying sugar juice, and have gained many successful experiences from resin decalcification, desalination, dealkalization to resin decoloration.
In the domestic sugar industry, resin decalcification is applied to sugar production, in recent years, southern sugarcane sugar enterprises are mainly used, northern beet sugar enterprises have been tested for resin decalcification, but because the technology is immature at the time, the production and operation cost is too high, resin regeneration waste liquid cannot be treated and other related factors, the application of resin decalcification in beet sugar production is insufficient, and no case is provided!
In the modern sugar beet sugar manufacturing production process, the sugar juice still contains a certain amount of calcium salt after the cleaning process, the calcium salt in the sugar juice can not be thoroughly removed by the existing sugar beet sugar manufacturing production process, or the content of the calcium salt in the sugar juice is effectively reduced, along with the progress of sugar manufacturing production, in the sugar juice evaporation process, the calcium salt in the sugar juice is gradually increased along with the concentration of the sugar juice, the calcium salt in the sugar juice is separated out from the sugar juice and is deposited on a heating pipe of sugar juice evaporation equipment, so that the heat exchange efficiency of the evaporation equipment is reduced, and the influence is directly caused on the balance and stability of sugar manufacturing production.
In order to reduce the influence of evaporator fouling on evaporation efficiency, the existing sugar production process adopts a mode of adding an anti-scaling agent into dilute juice to slow down the generation of the fouling of an evaporation tank, and because no food-grade anti-scaling agent exists at home and abroad at present, the anti-scaling agent needs to be removed in the subsequent production, so that the sugar production cost is increased; secondly, the food production safety problem is also involved; thirdly, the antiscaling agent is added into the sugar water, so that calcium ions in the sugar juice cannot be eliminated, and only the calcium ions are moved to the next procedure, so that the sensory quality of the finished sugar is reduced, the glossiness of the finished sugar is poor, and the turbidity of the finished sugar is increased seriously, thereby directly influencing the quality of the finished sugar.
Disclosure of Invention
The invention mainly solves the technical problems that calcium salt is difficult to remove in beet sugar production and the treatment difficulty of regenerated waste liquid is high when decalcifying resin is used for removing the calcium salt, and provides a beet sugar decalcification system, so that the stage of stopping production, cleaning and scaling can be saved in beet sugar production, and real continuous production can be realized.
The invention provides a beet sugar decalcification system, which adopts continuous multi-column ion exchange resin to remove calcium ions in beet sugar juice, and comprises:
a production area: including many ion exchange resin columns of parallelly connected setting, the beet sugar juice carries out ion exchange through the resin layer of many ion exchange resin columns of parallelly connected carrying out the decalcification back to beet sugar juice and obtains the thin juice that softens, and the drain pipe and the play feed tank of ion exchange resin column are connected. The discharge tank is used for discharging and caching the softened dilute juice, the pressure of the system for discharging is reduced, and the pump connected with the outlet of the discharge tank conveys the softened dilute juice to the evaporation working section.
Cooling the backwashing area: the method comprises the steps of switching a production area to a failure ion exchange resin column, and backwashing and cooling resin in the failure ion exchange resin column by softened dilute juice;
a regeneration zone: comprises an ion exchange resin column switched from a cooling backwashing area, and NaOH softened dilute juice regenerates resin in the ion exchange resin column after backwashing is finished;
leaching and preheating zone: comprises an ion exchange resin column switched from a regeneration zone, and the softened dilute juice is used for leaching and preheating the resin in the ion exchange resin column.
The ion exchange resin column in the production area adopts an upper feeding and lower discharging mode.
The lower part of the ineffective ion exchange resin column in the cooling backwashing area is connected with a compressed air pipeline, an exhaust pipe is arranged above the ineffective ion exchange resin column, an air valve is arranged on the compressed air pipeline, and compressed air is used for scrubbing the resin after the air valve is opened.
The regeneration zone comprises a plurality of ion exchange resin columns which are arranged in series, and a liquid outlet pipe of the regeneration zone is connected with the carbon pre-saturation tank. Because the regenerated liquid uses NaOH to soften dilute juice, the effluent of the ion exchange resin column is recycled to the tank before carbon saturation, and calcium ions can be discharged out of the system after precipitation and filtration are carried out.
The regeneration area feeding pipeline is provided with a pipeline mixer, and the inlet of the pipeline mixer is respectively connected with a sodium hydroxide solution inlet pipe and a softened dilute juice inlet pipe. The pipeline mixer can be used for preparing regeneration liquid NaOH softened dilute juice.
The leaching and preheating zone comprises a plurality of ion exchange resin columns which are arranged in series, and a top-in bottom-out mode is adopted during leaching in the leaching and preheating zone.
The leaching liquid outlet pipe is connected with the liquid inlet pipe of the regeneration zone in series. By connecting the rinse and preheat zones in series with the regeneration zone, the rinse can also be used in the regeneration zone, and therefore, the rinse can be fully utilized.
And after the elution of the ion exchange resin column in the first process position of the elution and preheating zone is finished, opening a backwashing inlet valve and introducing hot softening dilute juice to preheat the ion exchange resin column in the process position.
The single column volume of the ion exchange resin is 1.5-3m3。
The ion exchange resin column is Na type strong acid cation exchange resin column.
The beet sugar decalcification system can continuously produce, the ion exchange resin columns in the production area are switched out after being saturated, the ion exchange resin columns enter the cooling backwashing area to be switched to the regeneration area, the leaching area and the preheating area after being backwashed and cooled, the ion exchange resin columns in each working area are always kept unchanged in number through sequential switching, and beet sugar dilute juice can be continuously softened.
The decalcification ion exchange in the prior art 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 fixed bed treeWhen the fat adsorption saturation needs backwashing regeneration, the backwashing of the fixed bed resin can be realized only by needing larger flow. 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 dilute juice obtained by the beet sugar decalcification system enters the subsequent working procedures of an evaporator and the like, 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.
The system of the invention works on the principle that the system contains more Ca2+Passing the ionic disaccharide sugar juice (beet sugar juice) through a resin column filled with Na type cation resin to obtain Ca in the sugar juice2+Ions and Na in the resin layer+After ion exchange, the calcium ion content is reduced to a lower level, and a softened thin juice is obtained. Exchange more Ca2+Gradually lose the capacity to exchange, which we call spent resin. The sugar and calcium ions can form calcium sucrose (C) under alkaline conditions12H22O112CaO) soluble in water at a relatively low temperature (40 ℃). Dissolving NaOH in softened and decalcified clear juice (softened dilute juice) cooled to 40 deg.C, introducing into resin column to regenerate, reacting sucrose with Ca under such environmental conditions2+Form calcium sucrose (C)12H22O112CaO) solution, discharged to a carbon carbonation front tank along with regeneration effluent, subjected to a carbon carbonation process to precipitate sucrose and Ca2+The ions form a precipitate which is discharged through a carbon filtration system. The softened dilute juice is used as a carrier for systematic decalcification and resin regeneration, so that no regeneration waste liquid and waste regenerant are generated in systematic decalcification and resin regeneration, and no dilute juice is diluted, so that the influence on sugar production is avoided.
According to the modern sugar production process concept, a continuous multi-column ion exchange system is designed, and efficient intelligent automatic control is adopted to meet the continuous, balanced and stable production precondition of the sugar production process.
Beet, as the main raw material for sugar production of beet, is affected by soil moisture content, climatic conditions and planting technical reasons in the growth period, the natural quality presented by beet is different every year, and after the beet is harvested by beet processing enterprises, the processing quality of beet is changed along with the prolonging of the preservation time of beet and the difference of preservation technique and preservation condition; along with the increase of the processing period of the beet sugar production, the production process indexes are greatly fluctuated, which is concretely represented by that the calcium salt of the second clear juice is increased, the purity is reduced, and the color value is increased; particularly, the content of calcium salt in the second clear juice is gradually increased along with the extension of the production period and the change of the quality of the beet, so that the evaporation efficiency is reduced, the whole operation in the production season can be stable through the beet sugar decalcification system, and the effect can reach the design requirement.
Drawings
FIG. 1 is a process schematic diagram of a beet sugar decalcification system
FIG. 2 is a schematic diagram of the structure of the sugar beet decalcification system of the present invention.
FIG. 3 is a schematic diagram of the sugar beet decalcification system of example 1.
FIG. 4 is a front view of an ion exchange column of the present invention.
Detailed Description
The technical solution of the present invention will be explained in detail below.
The process schematic diagram of the beet sugar decalcification system of the invention is as shown in figure 1, and comprises the following procedures:
1) cleaning: carrying out carbon saturation and filtration treatment on the beet syrup stock solution;
2) the production process comprises the following steps: the sugar beet juice after the cleaning procedure is treated by Na type strong acid cation exchange resin to obtain softened dilute juice, and part of the softened dilute juice is sent into an evaporator for evaporation and concentration; in this step, Ca is contained+、K+、Na+The dilute juice stock solution is fed into Na type strong acid cation exchange resin for ion exchange to obtain softened dilute juice with Ca removed+The thin juice of (2);
3) and (3) backwashing: backwashing the saturated ion exchange resin absorbing calcium ions;
4) 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 ion exchange resin saturated with adsorbed calcium ions to regenerate the resin, and returning the regenerated liquid back to the raw material beet sugar dilute juice.
Before the regeneration process, the softened dilute juice is adopted to carry out backwashing on the decalcified ion exchange resin saturated by absorbing calcium ions. The temperature of the softened thin juice used for backwashing was 75-95 ℃. And after the regeneration process is finished, leaching the decalcified ion exchange resin by using softened dilute juice. After the leaching is finished, the leached decalcified ion exchange resin is preheated by using dilute juice at the temperature of 75-95 ℃.
The structure of the ion exchange resin column used in the beet sugar decalcification system of the invention is shown in FIG. 3:
the structure of the ion exchange resin column used in the beet sugar dilute juice softening method is shown in figure 3, (in order to save the position and fully utilize the space, a duplex column is generally used, the duplex column is two ion exchange resin columns which are arranged up and down, the duplex column is not communicated, as shown in figure 3), the ion exchange resin column comprises a shell 1, Na-type strong acid cation exchange resin is filled in the shell 1, the shell 1 is provided with an upper resin inlet 2, a lower resin outlet 3, a feed inlet 4 and a discharge outlet 5, 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 the top end and the bottom end of the inner part of each resin column shell 1 are provided with two resin distributors 8. The shell 1 is also provided with a reinforcing channel steel 9. The pipeline on the feed inlet 4 is provided with a valve which can allow materials, leacheate, backwash liquid, regeneration liquid and the like to enter, and the pipeline on the discharge outlet 5 is also provided with a valve which can allow materials, leacheate, backwash liquid, regeneration liquid and the like to exit.
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 deposit of 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.
As shown in FIG. 2, the sugar beet decalcification system of the present invention comprises a production zone 1, a cooling and backwashing zone 2, a regeneration zone 3, and a washing and preheating zone 4. 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 discharged CaO can be basically less than 10 mg/L.
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.
Example 1
As shown in FIG. 3, the present embodiment is designed as a 16-column, and the simulated movement of the ion exchange resin column is realized by switching the valve array, so as to continuously operate. 16 resin columns are distributed to process positions from 1# -16 #, which are respectively:
production area (1# -10 #): the method is characterized in that 10 resin columns are connected in parallel to run, beet sugar dilute juice is connected in parallel to perform ion exchange through the resin layers of the 10 resin columns to achieve the aim of decalcification, regenerated resin columns are switched into the area and are switched from the 10# process position to the 1# process position one by one, and the failure degree of the resin is gradually deepened until the resin fails; although 10 resin columns are used in the present embodiment, the number of resin columns in the production zone is not limited, and may be set according to the amount of material to be processed.
The feeding tank T-DC01 is connected with the resin column of the production area through a feeding pipe, a feeding pump P-DC01 is arranged on the feeding pipe, and the feeding pump P-DC01 conveys the beet sugar dilute juice to the production area of the system to complete ion exchange decalcification. The pipeline is also provided with a flow controller FCV-DC01, the flow controller FCV-DC01 controls and regulates the flow through a flow control loop, and the feeding pipeline is also provided with a temperature transmitter and a pressure transmitter.
The resin column of the production area is connected with a discharge tank T-DC02 through a discharge pipe, the softened thin juice of the beet sugar thin juice after ion exchange in the production area is conveyed to the discharge tank T-DC02, the discharge tank T-DC02 is used for discharging buffer storage of a thin juice decalcification system, the pressure of the system discharging is reduced, and a pump connected with the outlet of the discharge tank conveys the softened thin juice to an evaporation section.
Cooling the backwash zone (16 #): comprises 1 failed ion exchange resin column switched from production zone, and softened dilute juice is used for backwashing and cooling resin in the resin column, specifically, the failed resin column is switched from 1# process position to 16# position, and hot softened dilute juice is used for 25m3Flow rate backwash with cumulative volume set to 1m3(backwash effluent goes to the carbon hold-up tank through backwash effluent pipe); the resin was then back-flushed with air for 5 minutes to allow the resin to fully fluidize (each time the flushing was performed, the air vent valve was opened; then the hot softened dilute juice was used a second time at 25m3Flow rate backwash with cumulative volume set to 1m3(ii) a At 1.2m3The flow rate of the water is reversed to the cold (40 ℃) softened dilute juice, and the cumulative dosage is 0.5m3The resin is cooled down. (if the resin is properly fluidized and no caking is present, no air scrubbing is required and the time parameter is set to 0).
The discharge tank T-DC02 is connected with the resin column of the cooling and backwashing area through a hot material pipeline, and the heat softening dilute juice delivery pump P-DC02-2 is arranged on the hot material pipeline to deliver the hot softening dilute juice (80-90 ℃) to the resin column of the cooling and backwashing area to backwash the resin. The hot material pipeline is provided with a valve DC-99-05 to control the transportation of the hot softened dilute juice.
The discharge tank T-DC02 is connected with the resin column of the cooling and backwashing area through a cold material pipeline, the inlet of a cold softening dilute juice delivery pump P-DC02-1 is connected with the outlet of the discharge tank T-DC02, the outlet is connected with a cooling heat exchanger E-DC01, and the softened dilute juice is delivered to the resin column of the cooling and backwashing area through the cold material pipeline to cool the resin, wherein the cold softening dilute juice (40 ℃) is delivered to the resin column of the cooling and backwashing area through the cold material pipeline. The cold material pipeline is provided with a valve DC-99-06 for controlling the conveying of the cold softened dilute juice.
The inlet pipe of the resin column in the cooling and backwashing area is provided with a flow controller FCV-DC03 which can control the flow of the cold and hot softened dilute juice entering the resin column.
The compressed air is communicated with the lower part of the resin column through a pipeline, and an air valve DC-99-07 is arranged on the pipeline.
The resin column of the cooling backwashing area is connected with the resin backwashing tank through a pipeline. Specifically, the resin in the cooling backwash zone may be sent through a backwash line to a resin backwash tank for in vitro backwash.
Regeneration zone (13# -15 #): the number of the resin columns is set according to the production condition and is not limited to 3 in the embodiment. Specifically, after backwashing and cooling are finished on the resin column in the No. 16 process position, the resin column is switched to enter a regeneration zone, regeneration liquid is injected from the upper part of the column in the No. 13 process position in the regeneration zone, and is connected in series to the lower part of the column in the No. 15 process position, and then liquid is discharged to a carbon saturation front tank; the regenerated liquid entering the 13# is obtained by mixing and diluting softened dilute juice (40 ℃) washed by 12# and concentrated alkali with the concentration of 30% -50% through a pipeline by a pipeline mixer 10 at the 13# inlet, the alkali concentration reaches 4% -6%, and the total flow rate entering a column is 2.85m3The/h is the sum of the softened dilute juice washed from the washing zone of No. 11 to No. 12 and the concentrated alkali pumped by the concentrated alkali pump P-DC03, and the period cumulative volume is about 1.7m3. During this time, the valve of column # 13 was opened, and 200L of 30% NaOH was pumped in during this time, with the instantaneous flow being linear from column to columnThe steps are increased.
The alkali distribution tank is connected with the alkali tank T-DC03 through a pipeline, and a liquid alkali transfer pump P-DC05 is arranged on the pipeline to supplement the liquid alkali for regeneration from the alkali distribution tank to the alkali tank T-DC 03. The caustic tank T-DC03 was used to store the 30% -50% strength NaOH solution required for regeneration. The alkali tank T-DC03 is connected with the resin in the regeneration zone through a pipeline. The pipeline is also provided with a pressure transmitter and the like.
If the carbon pre-filling tank is arranged at a higher and/or farther position, a regeneration discharging transfer pump P-DC04 can be arranged on a regeneration discharging pipeline, and the pressure loss of the regeneration discharging pipeline can be reduced by the power transmission of the regeneration discharging transfer pump.
Rinsing and preheating zone (11# -12 #): the number of resin columns switched from the regeneration zone is set according to the production condition, and is not limited to 2 in the embodiment. Specifically, cold leaching is performed at the initial stage of cycle switching, softened dilute juice cooled to 40 ℃ by a cooling heat exchanger E-DC01 enters from the upper part of No. 11, is serially washed in the forward direction to the lower part of No. 12 and then is serially connected to a regeneration area, and the cold leaching and the regeneration are performed synchronously for about 0.6 hour. Preheating is carried out at the later stage of the period, other valves of the No. 11 process-level resin column are closed, backwashing is carried out by opening a backwashing inlet valve and a backwashing outlet valve, hot materials also enter the No. 11 process-level resin column from bottom to top through a heat softening dilute juice delivery pump P-DC02-2 to carry out preheating treatment on the resin, and the liquid outlet after the preheating treatment can be communicated with a two-carbon retention tank through a pipeline and has an instantaneous flow of 15m3H, cumulative volume 4.5m3。
An inlet of a cold softening dilute juice delivery pump P-DC02-1 is connected with an outlet of a discharge tank T-DC02, an outlet of the cold softening dilute juice delivery pump P-DC02-1 is connected with a cooling heat exchanger E-DC01, and the cold softening dilute juice (40 ℃) is delivered to a resin column in a leaching and preheating zone through a cold material pipeline to carry out cooling leaching on the resin. The inlet line of the resin column of the rinsing and preheating zone is provided with a flow controller FCV-DC 02.
Three outlets in the above system: the production area liquid outlet is provided with a production discharging resin catcher, the regeneration discharging port is provided with a regeneration discharging resin catcher, the backwashing discharging port is provided with a backwashing discharging resin catcher, and the resin catcher is a filter with a wedge-shaped filter screen and is used for simply filtering passing materials. The resin trap may trap resin that leaks out of the resin column. The amount of resin retained by the screen can be found by visual inspection. If a large amount of normal granular resin is trapped, the distributor of a certain resin column is damaged and leaked, and inspection and maintenance are needed; if only a small amount of broken resin exists, the distributor of the resin column is not leaked, when the trapped broken resin has influence on the discharge flow, the bypass valve is opened, the inlet and outlet valves are closed, then the valve is disassembled, then the bottom valve of the resin catcher is opened, and the broken resin can be recovered to be used after being discharged by back flushing. Normally, the bypass valve is normally closed.
The beet sugar decalcification system is adopted to treat beet sugar dilute juice, and the following indexes are achieved:
example 2 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, 200g of salt for regenerating resin per liter, and 10g of salt for removing 1g of CaO, wherein the dilute juice contains 20g of CaO per liter.
The experimental group adopts 6% NaOH softened dilute juice by mass percent as resin regeneration liquid, wherein each liter of resin regeneration NaOH136.8g contains CaO20g, and each liter of dilute juice consumes NaOH 7.1g when CaO 1g is removed.
The comparative indexes of the beet sugar decalcification regeneration method are as follows:
example 3 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 columns of 1.2m diameter were used, the resin packing volume of the entire system was 28m3About, the running linear velocity is 30m/h, and the flow rate of the material which can be fed is 340m3/h。
In a conventional fixed bed, when 2 large columns with a diameter of 3.45m are used, the resin packing volume of the whole system is still 28m3About, the running linear velocity is 30m/h, the flow rate of the material can be 280m3/h。
In comparison, it is clear that for the same resin loading, a multi-unit continuous ion exchange system is clearly capable of handling 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 sugar beet decalcification system comprising:
a production area: the device comprises a plurality of ion exchange resin columns which are arranged in parallel, beet sugar juice is subjected to ion exchange through resin layers of the plurality of ion exchange resin columns which are arranged in parallel to decalcify the beet sugar juice to obtain softened dilute juice, and a liquid outlet pipe of each ion exchange resin column is connected with a discharge tank;
cooling the backwashing area: the method comprises the steps of switching a production area to a failure ion exchange resin column, and backwashing and cooling resin in the failure ion exchange resin column by softened dilute juice;
a regeneration zone: comprises an ion exchange resin column switched from a cooling backwashing area, and NaOH softened dilute juice regenerates resin in the ion exchange resin column after backwashing is finished;
leaching and preheating zone: comprises an ion exchange resin column switched from a regeneration zone, and the softened dilute juice is used for leaching and preheating the resin in the ion exchange resin column.
2. The sugar beet decalcification system of claim 1, wherein the ion exchange resin column of the production zone is top-feed bottom-discharge.
3. The sugar beet decalcification system of claim 1, wherein the lower part of the spent ion exchange resin column in the cooling and backwashing area is connected with a compressed air pipeline, an exhaust pipe is arranged above the spent ion exchange resin column, an air valve is arranged on the compressed air pipeline, and the compressed air cleans the resin after the air valve is opened.
4. The sugar beet decalcification system of claim 1, wherein the regeneration zone comprises a plurality of ion exchange resin columns arranged in series, and the effluent pipe of the regeneration zone is connected to the carbon pre-carbonation tank.
5. The sugar beet decalcification system of claim 1, wherein a pipeline mixer is provided on the regeneration zone feed pipeline, the inlet of the pipeline mixer being connected to the sodium hydroxide solution inlet pipe and the softened thin juice inlet pipe, respectively.
6. The sugar beet decalcification system of claim 1, wherein the washing and preheating zone comprises a plurality of ion exchange resin columns arranged in series, wherein the washing and preheating zone uses a top-in-bottom-out mode.
7. The sugar beet sugar decalcification system of claim 6, wherein the effluent rinse line is connected in series with the regeneration zone inlet line.
8. The sugar beet decalcification system of claim 6, wherein the ion exchange resin column of the first process location of the washing and preheating zone is preheated after washing by opening the backwash and backwash inlet valve to introduce the heat softened dilute juice.
9. The sugar beet sugar decalcification system according to claim 1,the single column volume of the ion exchange resin is 1.5-3m3。
10. The sugar beet decalcification system of claim 1, wherein the ion exchange resin column is a Na-type strong acid cation exchange resin column.
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| CN202111235828.1A CN114277196A (en) | 2021-10-22 | 2021-10-22 | Beet sugar decalcification system |
| CN202210525588.7A CN114606350A (en) | 2021-10-22 | 2022-05-16 | Beet sugar decalcification system |
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| CN115595383B (en) * | 2022-08-31 | 2024-07-26 | 新疆冠农股份有限公司 | Syrup dilute juice decalcification process |
| CN121130962B (en) * | 2025-11-18 | 2026-02-06 | 欧尚元智能装备股份有限公司 | Sugarcane juice decalcification resin regeneration solution treatment method and sugarcane juice decalcification method |
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| GB900642A (en) * | 1957-07-25 | 1962-07-11 | Nippon Beet Sugar Mfg | Process for the purification of beet sugar juice |
| 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 |
| FR3094724B1 (en) * | 2019-04-05 | 2021-04-23 | Novasep Process | Sugar processing process |
| CN111450903B (en) * | 2020-05-21 | 2024-09-10 | 浙江华康药业股份有限公司 | Continuous ion exchange system for xylose production and application method thereof |
| CN112593016A (en) * | 2020-12-22 | 2021-04-02 | 新疆冠农果茸股份有限公司 | Process for preparing high-quality white granulated sugar and fulvic acid dry powder from beet |
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