CN115595383A - Process for decalcifying syrup thin juice - Google Patents
Process for decalcifying syrup thin juice Download PDFInfo
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- CN115595383A CN115595383A CN202211059611.4A CN202211059611A CN115595383A CN 115595383 A CN115595383 A CN 115595383A CN 202211059611 A CN202211059611 A CN 202211059611A CN 115595383 A CN115595383 A CN 115595383A
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- juice
- dilute
- syrup
- decalcifying
- decalcified
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- 235000011389 fruit/vegetable juice Nutrition 0.000 title claims abstract description 173
- 238000000034 method Methods 0.000 title claims abstract description 81
- 239000006188 syrup Substances 0.000 title claims abstract description 73
- 235000020357 syrup Nutrition 0.000 title claims abstract description 73
- 239000011347 resin Substances 0.000 claims abstract description 49
- 229920005989 resin Polymers 0.000 claims abstract description 49
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 45
- 238000011001 backwashing Methods 0.000 claims abstract description 23
- 230000008929 regeneration Effects 0.000 claims abstract description 23
- 238000011069 regeneration method Methods 0.000 claims abstract description 23
- 239000000243 solution Substances 0.000 claims abstract description 22
- 238000001914 filtration Methods 0.000 claims abstract description 16
- 238000002156 mixing Methods 0.000 claims abstract description 15
- 238000001816 cooling Methods 0.000 claims abstract description 14
- 239000011259 mixed solution Substances 0.000 claims abstract description 13
- 238000005086 pumping Methods 0.000 claims abstract description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 17
- 239000003365 glass fiber Substances 0.000 claims description 8
- 238000010992 reflux Methods 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 6
- 239000003513 alkali Substances 0.000 claims description 2
- 239000003518 caustics Substances 0.000 claims description 2
- 239000011148 porous material Substances 0.000 claims 1
- 239000002002 slurry Substances 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 13
- 238000006243 chemical reaction Methods 0.000 abstract description 6
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract description 5
- 239000011575 calcium Substances 0.000 abstract description 5
- 229910052791 calcium Inorganic materials 0.000 abstract description 5
- 235000013379 molasses Nutrition 0.000 abstract description 4
- 230000000052 comparative effect Effects 0.000 description 27
- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 description 17
- 229930006000 Sucrose Natural products 0.000 description 17
- 239000005720 sucrose Substances 0.000 description 17
- 239000011162 core material Substances 0.000 description 7
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 4
- 150000001768 cations Chemical class 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- 229910052708 sodium Inorganic materials 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 159000000007 calcium salts Chemical class 0.000 description 2
- 125000002091 cationic group Chemical group 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 235000016068 Berberis vulgaris Nutrition 0.000 description 1
- 241000335053 Beta vulgaris Species 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- CZMRCDWAGMRECN-UHFFFAOYSA-N Rohrzucker Natural products OCC1OC(CO)(OC2OC(CO)C(O)C(O)C2O)C(O)C1O CZMRCDWAGMRECN-UHFFFAOYSA-N 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 235000015191 beet juice Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 239000008395 clarifying agent Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 235000012907 honey Nutrition 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000002455 scale inhibitor Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D35/00—Filtering devices having features not specifically covered by groups B01D24/00 - B01D33/00, or for applications not specifically covered by groups B01D24/00 - B01D33/00; Auxiliary devices for filtration; Filter housing constructions
- B01D35/16—Cleaning-out devices, e.g. for removing the cake from the filter casing or for evacuating the last remnants of liquid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D36/00—Filter circuits or combinations of filters with other separating devices
- B01D36/003—Filters in combination with devices for the removal of liquids
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Biochemistry (AREA)
- Non-Alcoholic Beverages (AREA)
Abstract
The invention relates to the technical field of molasses processing, and discloses a process for decalcifying dilute syrup juice, which is characterized by comprising the following steps: (1) Performing resin exchange on the syrup dilute juice by a decalcification column, and filtering by a filter to obtain decalcification dilute juice; (2) Pumping the decalcified dilute juice obtained in the step (1) into a decalcifying column through a backwashing pump to carry out backwashing on the decalcifying column; (3) Cooling the decalcified dilute juice obtained in the step (1), mixing with a NaOH solution, and conveying the obtained mixed solution into a decalcification column for resin regeneration; the syrup dilute juice decalcification process can effectively reduce the calcium content in the dilute juice, further reduce the sugar juice turbidity, reduce the scaling damage in a reaction container in the sugar juice concentration process, reduce the steam consumption, improve the filterability of the concentrated juice, provide softened sugar juice with better quality for downstream production, further improve the sugar quality, reduce the production cost, optimize the production performance of the whole sugar production and improve the yield.
Description
Technical Field
The invention relates to the technical field of molasses processing, in particular to a process for decalcifying syrup dilute juice.
Background
Lime is often used as a neutralizing agent and a clarifying agent in a sugar refinery, and due to incomplete clarification, part of calcium salt is left in dilute juice, and the calcium salt can increase the scaling of an evaporation tank and the honey making coefficient during the next sugar boiling, so that the sugar recovery rate is reduced. By using the traditional beet sugar production process, the production yield of molasses, the purity, the quality, the energy and the like of sugar are all influenced by residual calcium in beet juice, although the dilute juice decalcification technology has been used for many years, the traditional dilute juice decalcification technology is not widely applicable, the consumption of chemicals is high, and the subsequent sewage cleaning process causes outstanding environmental problems.
Therefore, how to provide a low residual calcium content, low energy consumption, green and environmental-friendly syrup dilute juice decalcification process is a technical problem to be solved by those skilled in the art.
Disclosure of Invention
In view of the above, the invention provides a syrup dilute juice decalcification process, which aims to solve the problems that the production yield and purity of molasses are affected by residual calcium in syrup dilute juice, and the phenomena of high consumption of chemicals and serious environmental pollution in the traditional dilute juice decalcification process.
In order to solve the technical problems, the invention adopts the following technical scheme:
a process for decalcifying syrup dilute juice comprises the following steps:
(1) Performing resin exchange on the syrup dilute juice by a decalcification column, and filtering by a filter to obtain decalcification dilute juice;
(2) Pumping the decalcified dilute juice obtained in the step (1) into a decalcifying column through a backwashing pump to carry out backwashing on the decalcifying column;
(3) And (2) cooling the decalcified dilute juice obtained in the step (1), mixing with a NaOH solution, and conveying the obtained mixed solution into a decalcifying column for resin regeneration.
Preferably, in the syrup dilute juice decalcification process, the resin in the step (1) is a strong cationic resin.
Compared with the traditional process, the strong cationic resin adopted by the invention is economical and practical, has lower expansion/shrinkage rate, and has smaller mechanical stress, longer service life and low operation cost.
Preferably, in the syrup dilute juice decalcification process, the concentration of the syrup dilute juice in the step (1) is 100-250mg/L, and more preferably 100mg/L; the feeding temperature is not more than 90 ℃, and further preferably 70-78 ℃; the sucrose concentration is 15-16%.
Preferably, in the above process for decalcifying dilute syrup, the syrup in step (1)The speed of the dilute juice entering the decalcification column is 225-235m 3 H, more preferably 225m 3 /h。
Preferably, in the syrup dilute juice decalcification process, the filter in the step (1) is a cartridge filter, the aperture of the cartridge filter is 0.1 μm, and the filter core is made of glass fiber and/or activated carbon;
further preferably, in the syrup dilute juice decalcification process, the cartridge filter is provided with a first security filter and a second security filter, and the input end of the second security filter is connected with the output end of the first security filter; wherein the aperture of the first safety filter is 0.1 μm, and the filter core is made of glass fiber; the aperture of the second cartridge filter is 0.1 μm, and the filter core is made of active carbon.
Preferably, in the above process for decalcifying dilute syrup juice, the decalcified dilute syrup juice in step (2) has a thickness of 8-15m 3 The flow rate of the decalcification solution is pumped into the decalcification column for backwashing, and further preferably, the decalcification dilute juice is pumped into the decalcification column at a flow rate of 10m 3 And pumping the filtrate at a flow rate of/h into the decalcification column for backwashing the decalcification column.
Preferably, in the process of decalcifying the dilute syrup juice, the cooling in step (3) is to cool the decalcified dilute juice to below 28 ℃, and more preferably to 20-25 ℃.
Preferably, in the syrup dilute juice decalcification process, the mixed solution in the step (3) is a 4-6 vol% NaOH solution prepared from the decalcified dilute juice as a solvent and 50% caustic alkali as a solute.
Preferably, in the syrup dilute juice decalcification process, the addition rate of the NaOH solution in the step (3) is 45-50kg/h, and more preferably 47.8kg/h.
Preferably, in the syrup dilute juice decalcification process, a single-channel decalcification device is adopted in the decalcification process, the concurrent flow is a dilute juice decalcification process, the duration is at least 12h, the countercurrent flow is a resin regeneration process, the duration is not more than 12h, and each period is preset to be 24h.
Preferably, in the process of decalcifying the dilute syrup juice, the method further comprises the following steps:
(4) Pumping the decalcified dilute juice obtained in the step (1) into a decalcifying column through a backwashing pump to drip wash the regenerated decalcifying column;
(5) And (4) refluxing the washed decalcified dilute juice to a syrup dilute juice storage tank for circulating and carrying out the steps (1) - (4).
The invention provides a process for decalcifying syrup dilute juice, which has the following beneficial effects compared with the prior art:
by adopting the syrup dilute juice decalcification process, the energy consumption can be effectively reduced, the evaporator does not need to be cleaned during the season of squeezing, the steam consumption can be reduced, the production stop caused by cleaning the evaporator can not occur, the evaporator with smaller capacity can be used, the energy consumption is saved by 5-15 percent, and the use of a large amount of scale inhibitors is effectively avoided;
by adopting the syrup dilute juice decalcification process, the calcium content in the dilute juice can be effectively reduced, the sugar juice turbidity is further reduced, the harm of scaling in a reaction container in the sugar juice concentration process is reduced, the steam consumption is reduced, the filterability of the concentrated juice is improved, softened sugar juice with better quality is provided for downstream production, the sugar quality is further improved, the production cost is reduced, the production performance of the whole sugar production is optimized, and the yield is improved;
the syrup thin juice process of the invention has the advantages of no need of cooling, no acid consumption, no raw sugar loss, no resin hydrolysis, no sewage discharge and environmental protection.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.
Example 1
The embodiment provides a syrup dilute juice decalcification process, which comprises the following steps:
(1) Mixing syrup dilute juice with CaO content of 100mg/L, temperature of 75 deg.C, sucrose concentration of 15-16%, and suspended matter concentration of 50mg/LAt 225m 3 The reaction solution is conveyed into a decalcification column at a speed of/h for resin exchange, wherein the resin is strong cation sodium type resin;
(2) Conveying the syrup dilute juice subjected to resin exchange to a first security filter with the aperture of 0.1 mu m and a filter element made of glass fiber for filtration, and then continuously conveying the syrup dilute juice to a second security filter with the aperture of 0.1 mu m and a filter element made of activated carbon for filtration to obtain decalcified dilute juice;
(3) The decalcified dilute juice obtained in the step (1) is added by 10m 3 Pumping the flow velocity of the flow velocity/h into the decalcification column through a backwashing pump to perform backwashing on the decalcification column;
(4) Cooling the decalcified dilute juice obtained in the step (1) to 25 ℃ through a heat exchanger, then mixing the cooled decalcified dilute juice with a NaOH solution with the volume concentration of 4-6%, and conveying the obtained mixed solution into a decalcification column at the rate of 47.8kg/h for resin regeneration;
(5) After the resin regeneration process is finished, pumping the decalcified dilute juice obtained in the step (2) into the decalcifying column through a backwashing pump to drip wash the regenerated decalcifying column;
(6) And (5) refluxing the washed decalcified dilute juice to a syrup dilute juice storage tank for circulating and carrying out the steps (1) - (5).
The performance of the decalcified thin juice obtained after the treatment by the continuous decalcification process is detected, and the result is as follows: the decalcified dilute juice has CaO content of 9.1mg/L, temperature of 85 deg.C, sucrose concentration of 15-16%, and suspended matter concentration of 15mg/L.
Example 2
A process for decalcifying syrup dilute juice comprises the following steps:
(1) Mixing syrup dilute juice with CaO content of 150mg/L, temperature of 70 deg.C, sucrose concentration of 15-16%, and suspended matter concentration of 50mg/L at 225m 3 The reaction solution is conveyed into a decalcification column at a speed of/h for resin exchange, wherein the resin is strong cation sodium type resin;
(2) Conveying the syrup thin juice subjected to resin exchange to a cartridge filter with the aperture of 0.1 mu m and the filter core material of activated carbon for filtering to obtain decalcified thin juice;
(3) The decalcified dilute juice obtained in the step (1) is added with 12m 3 Flow rate per hour throughThe backwashing pump pumps the decalcification column into the decalcification column to perform backwashing on the decalcification column;
(4) Cooling the decalcified dilute juice obtained in the step (1) to 28 ℃ through a heat exchanger, then mixing the cooled decalcified dilute juice with a NaOH solution with the volume concentration of 4-6%, and conveying the obtained mixed solution into a decalcification column at the speed of 45kg/h for resin regeneration;
(5) After the resin regeneration process is finished, pumping the decalcified dilute juice obtained in the step (2) into the decalcifying column through a backwashing pump to drip wash the regenerated decalcifying column;
(6) And (5) refluxing the washed decalcified dilute juice to a syrup dilute juice storage tank for circulating and carrying out the steps (1) - (5).
The performance of the decalcified thin juice obtained after the treatment by the continuous decalcification process is detected, and the result is as follows: the decalcified dilute juice has CaO content of 15.2mg/L, temperature of 77 deg.C, sucrose concentration of 15-16%, and suspended matter concentration of 28mg/L.
Example 3
The embodiment provides a syrup dilute juice decalcification process, which comprises the following steps:
(1) Mixing syrup dilute juice with CaO content of 200mg/L, temperature of 80 deg.C, sucrose concentration of 15-16%, and suspended matter concentration of 50mg/L at 225m 3 The reaction solution is conveyed into a decalcification column at a speed of/h for resin exchange, wherein the resin is strong cation sodium type resin;
(2) Conveying the syrup dilute juice subjected to resin exchange to a first security filter with the aperture of 0.1 mu m and a filter element made of glass fiber for filtering, and then continuously conveying the syrup dilute juice to a second security filter with the aperture of 0.1 mu m and a filter element made of activated carbon for filtering to obtain decalcified dilute juice;
(3) Adding the decalcified dilute juice obtained in the step (1) to 8m 3 Pumping the flow velocity of the flow velocity/h into the decalcification column through a backwashing pump to perform backwashing on the decalcification column;
(4) Cooling the decalcified dilute juice obtained in the step (1) to 20 ℃ through a heat exchanger, then mixing the cooled decalcified dilute juice with a NaOH solution with the volume concentration of 4-6%, and conveying the obtained mixed solution into a decalcification column at the speed of 48kg/h for resin regeneration;
(5) After the resin regeneration process is finished, pumping the decalcified dilute juice obtained in the step (2) into the decalcifying column through a backwashing pump to drip wash the regenerated decalcifying column;
(6) And (5) refluxing the washed decalcified dilute juice to a syrup dilute juice storage tank for circulating and carrying out the steps (1) - (5).
The performance of the decalcified thin juice obtained after the treatment by the continuous decalcification process is detected, and the result is as follows: the decalcified dilute juice has CaO content of 18.8mg/L, temperature of 92 deg.C, sucrose concentration of 15-16%, and suspended matter concentration of 16mg/L.
Example 4
The embodiment provides a process for decalcifying syrup dilute juice, which comprises the following steps:
(1) Mixing syrup dilute juice with CaO content of 250mg/L, temperature of 90 deg.C, sucrose concentration of 15-16%, and suspended matter concentration of 50mg/L at 225m 3 The reaction solution is conveyed into a decalcification column at a speed of/h for resin exchange, wherein the resin is strong cation sodium type resin;
(2) Conveying the syrup dilute juice subjected to resin exchange to a cartridge filter with the aperture of 0.1 mu m and the filter core material of active carbon for filtering to obtain decalcified dilute juice;
(3) The decalcified dilute juice obtained in the step (1) is added with the weight of 15m 3 Pumping the flow velocity of the flow velocity/h into the decalcification column through a backwashing pump to perform backwashing on the decalcification column;
(4) Cooling the decalcified dilute juice obtained in the step (1) to 23 ℃ through a heat exchanger, then mixing the cooled decalcified dilute juice with a NaOH solution with the volume concentration of 4-6%, and conveying the obtained mixed solution into a decalcification column at the speed of 50kg/h for resin regeneration;
(5) After the resin regeneration process is finished, pumping the decalcified dilute juice obtained in the step (2) into the decalcifying column through a backwashing pump to drip wash the regenerated decalcifying column;
(6) And (5) refluxing the washed decalcified dilute juice to a syrup dilute juice storage tank for circulating and carrying out the steps (1) - (5).
The decalcification process of the embodiment of the invention adopts a single-channel decalcification device, wherein forward flow is a dilute juice decalcification process, the duration is at least 12h, reverse flow is a resin regeneration process, the duration is not more than 12h, each period is preset to be 24h, and the beet treatment capacity can reach 4500 tons/day.
The performance of the decalcified thin juice obtained after the treatment by the continuous decalcification process is detected, and the result is as follows: the decalcified dilute juice contains CaO 20.5mg/L, sucrose 15-16% and suspended matter 30mg/L at 95 deg.c.
Comparative example 1
Comparative example 1 a process for decalcifying a thin syrup juice is provided, comparative example 1 being substantially the same as example 1 except that:
(2) And (3) conveying the syrup thin juice subjected to resin exchange to a cartridge filter with the aperture of 0.1 mu m and the filter core material of glass fiber for filtering to obtain the decalcified thin juice.
The performance of the decalcified dilute juice obtained after treatment by the continuous decalcification process of the comparative example 1 was tested, and the results were as follows: the decalcified dilute juice contains CaO 9.8mg/L, sucrose 15-16% at 81 deg.C, and suspended matter 45mg/L.
Comparative example 2
Comparative example 2 provides a process for decalcifying a thin syrup juice, comparative example 2 being substantially the same as example 1 except that:
(2) And (3) conveying the syrup dilute juice subjected to resin exchange to a first security filter with the aperture of 0.1 mu m and the filter element made of activated carbon for filtration, and then continuously conveying the syrup dilute juice to a second security filter with the aperture of 0.1 mu m and the filter element made of glass fiber for filtration to obtain the decalcified dilute juice.
The performance of the decalcified dilute juice obtained by detecting the decalcified dilute juice after the treatment by the continuous decalcification process has the following results: the decalcified dilute juice has CaO content of 9.6mg/L, temperature of 86 deg.C, sucrose concentration of 15-16%, and suspended matter concentration of 43mg/L.
Comparative example 3
Comparative example 3 a process for decalcifying a thin syrup juice is provided, comparative example 3 being substantially the same as example 1 except that:
(2) And (3) conveying the syrup dilute juice subjected to resin exchange to a cartridge filter with the aperture of 0.1 mu m and the filter core material of active carbon for filtering to obtain the decalcified dilute juice.
The performance of the decalcified thin juice obtained after the treatment by the continuous decalcification process is detected, and the result is as follows: the decalcified dilute juice contains CaO 9.1mg/L, sucrose 15-16% at 82 deg.C, and suspended matter 21mg/L.
Comparative example 4
Comparative example 4 provides a process for decalcifying a thin syrup juice, comparative example 4 being substantially the same as example 1 except that: the resin-exchanged syrup thin juice is not subjected to the filtering operation but directly subjected to the subsequent steps.
The performance of the decalcified dilute juice obtained by detecting the decalcified dilute juice after the treatment by the continuous decalcification process has the following results: the decalcified dilute juice contains CaO 10.2mg/L, sucrose 15-16% and suspended matter 50mg/L at 80 deg.C.
From the results of comparative examples 1 to 4, it can be seen that the filtering operation can effectively remove suspended matters in the syrup thin juice, and has a certain gain effect on the reduction of the CaO content, and the syrup thin juice treated by the glass fiber cartridge filter and the activated carbon cartridge filter in sequence can achieve better effect.
Comparative example 5
Comparative example 5 provides a process for decalcifying a thin syrup juice, comparative example 5 being substantially the same as example 1 except that:
(4) And (2) cooling the decalcified dilute juice obtained in the step (1) to 18 ℃ through a heat exchanger, then mixing the cooled decalcified dilute juice with a NaOH solution with the volume concentration of 4-6%, and conveying the obtained mixed solution into a decalcification column at the speed of 47.8kg/h for resin regeneration.
The performance of the decalcified dilute juice obtained by detecting the decalcified dilute juice after the treatment by the continuous decalcification process has the following results: the decalcified dilute juice has CaO content of 25.2mg/L, temperature of 85 deg.C, sucrose concentration of 15-16%, and suspended matter concentration of 19mg/L.
Comparative example 6
Comparative example 6 provides a process for decalcifying a thin syrup juice, comparative example 6 being substantially identical to example 1 except that:
(4) And (2) cooling the decalcified dilute juice obtained in the step (1) to 20 ℃ through a heat exchanger, then mixing the cooled decalcified dilute juice with a NaOH solution with the volume concentration of 4-6%, and conveying the obtained mixed solution into a decalcification column at the rate of 47.8kg/h for resin regeneration.
The performance of the decalcified thin juice obtained after the treatment by the continuous decalcification process is detected, and the result is as follows: the decalcified dilute juice has CaO content of 10.3mg/L, temperature of 85 deg.C, sucrose concentration of 15-16%, and suspended matter concentration of 16mg/L.
Comparative example 7
Comparative example 7 provides a process for decalcifying a thin syrup juice, comparative example 7 being substantially the same as example 1 except that:
(4) Cooling the decalcified dilute juice obtained in the step (1) to 28 ℃ through a heat exchanger, then mixing the cooled decalcified dilute juice with a NaOH solution with the volume concentration of 4-6%, and conveying the obtained mixed solution into a decalcification column at the speed of 47.8kg/h for resin regeneration;
the performance of the decalcified thin juice obtained after the treatment by the continuous decalcification process is detected, and the result is as follows: the decalcified dilute juice has CaO content of 12.1mg/L, temperature of 84 deg.C, sucrose concentration of 15-16%, and suspended matter concentration of 14mg/L.
Comparative example 8
Comparative example 8 provides a process for decalcifying a thin syrup juice, comparative example 8 being substantially identical to example 1 except that:
(4) Cooling the decalcified dilute juice obtained in the step (1) to 30 ℃ through a heat exchanger, then mixing the cooled decalcified dilute juice with a NaOH solution with the volume concentration of 4-6%, and conveying the obtained mixed solution into a decalcification column at the speed of 47.8kg/h for resin regeneration;
the performance of the decalcified thin juice obtained after the treatment by the continuous decalcification process is detected, and the result is as follows: the decalcified dilute juice has CaO content of 24.8mg/L, temperature of 85 deg.C, sucrose concentration of 15-16%, and suspended matter concentration of 21mg/L.
From comparative examples 5 to 8, it can be seen that the temperature of the decalcified juice used in the resin regeneration process has important effects on the CaO content, the suspended matter concentration, etc. in the final decalcified juice, and when the temperature is too high or too low, the CaO content and the suspended matter concentration are increased, and the reason for this result is probably because the temperature of the decalcified juice affects the resin regeneration degree, and if the resin regeneration is not complete, the decalcifying effect of the syrup juice in the continuous decalcifying process is affected.
In conclusion, the filtration operation and the temperature control of the decalcified dilute juice used for resin regeneration have important influence on the CaO content and the suspended matter concentration in the finally obtained decalcified dilute juice, the invention does not relate to the consumption of water, the decalcified dilute juice is recycled, the energy consumption is saved, the cost is reduced, and because the invention adopts two decalcified columns for circulating operation, the operation progress cannot be influenced by the resin regeneration and cleaning processes, the production efficiency is greatly improved, and the invention conforms to the concept of energy conservation and environmental protection
The embodiments in the present description are described in a progressive manner, each embodiment focuses on differences from other embodiments, and the same and similar parts among the embodiments are referred to each other. For the scheme disclosed by the embodiment, the scheme corresponds to the method disclosed by the embodiment, so that the description is simple, and the relevant points can be referred to the method part for description.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (10)
1. The process for decalcifying the syrup dilute juice is characterized by comprising the following steps of:
(1) Performing resin exchange on the syrup dilute juice by a decalcification column, and filtering by a filter to obtain decalcification dilute juice;
(2) Pumping the decalcified dilute juice obtained in the step (1) into a decalcifying column through a backwashing pump to carry out backwashing on the decalcifying column;
(3) And (2) cooling the decalcified dilute juice obtained in the step (1), mixing with a NaOH solution, and conveying the obtained mixed solution into a decalcifying column for resin regeneration.
2. The process for decalcifying a dilute juice syrup according to claim 1, wherein the dilute juice syrup in step (1) has a concentration of 100 to 250mg/L and a feeding temperature of not more than 90 ℃.
3. The process of claim 1, wherein the rate of entry of the syrup slurry into the decalcifying column in step (1) is 225-235m 3 /h。
4. The process of claim 1, wherein the filter in step (1) is a cartridge filter, the pore size of the cartridge filter is 0.1 μm, and the filter core is made of glass fiber and/or activated carbon.
5. The process for decalcifying dilute syrup juice according to claim 1, wherein in the step (2), the decalcified dilute juice is present in a range of 8 to 15m 3 The flow rate of the decalcification column is pumped into the decalcification column for backwashing.
6. The process of claim 1, wherein the cooling step (3) is carried out to cool the decalcified juice to a temperature below 28 ℃.
7. The process of claim 1, wherein the mixed solution in step (3) is a 4-6 vol.% NaOH solution prepared from the decalcified juice solution and 50 vol.% caustic alkali as solute.
8. The process for decalcifying a dilute syrup according to claim 1, wherein the rate of addition of NaOH solution in step (3) is 45-50kg/h.
9. The process of claim 1, wherein the decalcification process comprises a single-channel decalcification apparatus, concurrent flow is a dilute juice decalcification process with a duration of at least 12h, and countercurrent flow is a resin regeneration process with a duration of no more than 12h, and each cycle is preset to 24h.
10. A process of decalcifying a thin syrup according to any one of claims 1 to 9, further comprising the steps of:
(4) Pumping the decalcified dilute juice obtained in the step (1) into a decalcifying column through a backwashing pump to drip wash the regenerated decalcifying column;
(5) And (4) refluxing the washed decalcified dilute juice to a syrup dilute juice storage tank for circulating and carrying out the steps (1) - (4).
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