CN104004860A - Production process and device of golden sugar - Google Patents
Production process and device of golden sugar Download PDFInfo
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- CN104004860A CN104004860A CN201410235021.1A CN201410235021A CN104004860A CN 104004860 A CN104004860 A CN 104004860A CN 201410235021 A CN201410235021 A CN 201410235021A CN 104004860 A CN104004860 A CN 104004860A
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Abstract
The invention provides a production process and a production device of golden sugar. The production process comprises the following steps: pressing sugarcane or beets to obtain cane sugar juice; pre-filtering the cane sugar juice through a coarse filter and feeding the pre-filtered crane sugar juice into a microfiltration membrane for filtering to obtain clear cane sugar juice; pre-concentrating the clear cane sugar juice to obtain a pre-concentrated solution; feeding the pre-concentrated solution into ion exchange resin for desalting to obtain a permeation solution; feeding the permeation solution into an evaporator for concentrating to obtain cane sugar concentrated liquid; heating the cane sugar concentrated liquid to be oversaturated, adding crystal seeds, naturally cooling and crystallizing, and centrifuging the obtained crystals to obtain golden sugar crystals; drying the golden sugar crystals to obtain a finished product of the golden sugar. The production device comprises the coarse filter, a microfiltration membrane filter, a nanofiltration membrane filter, an anion exchange resin bed, a cation exchange resin bed and the evaporator which are connected in sequence. The production method provided by the invention is capable of continuously producing high-quality golden sugar, the chromatic value of the obtained product is 800-3,000, the desalting rate is high, and the yield is high.
Description
Technical field
The invention belongs to sugar refining field, be specifically related to a kind of production technique and device of yellow gold sugar.
Background technology
Yellow gold sugar, is also brown sugar, gold sand sugar, be contain certain nutritive ingredient be not with sweet granulated sugar.It is faint yellow that color and luster is.Its production technique and white sugar are similar, but also not exclusively filter in process of production the nutritive substance of the inside, so it has preserved part sugarcane fragrance and nutrition, and have retained a lot of natural mineral matters.
Along with improving constantly of Chinese people people production level, people are to the consumption of sugar also diversification day by day.In recent years, also increasing year by year in the eating requirements of the ground brown sugars such as northern China.Therefore,, in the Guangxi, main Chan Tang district of China, there is the middle-size and small-size sugar refinery of part squeezing the initial stage of producing in season or entirely squeezing season and produce brown sugar.For the higher initial stage in squeezing season of reducing sugar, the sugar yield of producing brown sugar is relatively high, both can obtain good economic benefit, can satisfy the demands of consumers again.But it is mainly the production with reference to raw sugar that brown sugar is produced cleaning technique, taking lime method as main, production process sulfurous gas bleaching, contains sulphur residual in product.Must on the basis of lime method, improve, just can make equipment can adapt to production brown sugar, the natural flavor that the while also can retained product sugar.
The technique of domestic production yellow gold sugar is mainly taking lime method as main at present, has introduced new salinity, and in the time of full charge, precipitation, syrup is not clarified, and has not effectively removed the material such as mud juice, colloid in syrup.Cause product purity not high, mouthfeel is poor.Also there is more shortcoming in this technique: first, its technique will adopt lime precipitation removal of impurities, after natural sedimentation or filter press, can produce a large amount of residues, and environmental pollution is more serious; Secondly, in the method, using is that lime needs calcining, has consumed larger energy on the one hand and with waste discharge, has also increased an operation section simultaneously, increases production cost; The 3rd, this product, through long high temperature evaporation, produces Maillard reaction, and the pigment in its product is not natural pigment, and human body be there is no to benefit; The 4th, the concentration technology of the method adopts multiple-effect evaporator, and energy consumption is higher, and production cost is high; The 5th, this technique is relatively numerous and diverse, and equipment is many, control complex process, and floor space is large, and capital construction cost is also high.The 6th, this technique does not have the operation section of desalination,
In view of this, still await proposing a kind of production technique of improved yellow gold sugar.
Summary of the invention
The object of the present invention is to provide a kind of production technique and device of yellow gold sugar, directly, taking sugarcane or beet as raw material, continuously produce high-quality gold sugar, the colourimetric number of products obtained therefrom 800～3000, ratio of desalinization is high, yield is high.
A production technique for yellow gold sugar, comprises the following steps:
Step 1, squeezes sugarcane or beet by draining device, obtain sucrose mix juice;
Step 2, is undertaken step 1 gained sucrose mix juice after pre-filtering by coarse filter, then sends into microfiltration membrane and filter, and obtains sucrose mix juice clear liquid;
Step 3, carries out pre-concentration by step 2 gained sucrose mix juice clear liquid, makes the volume of sucrose mix juice clear liquid be concentrated into 30%～40%, obtains pre-concentration liquid;
Step 4, sends step 3 gained pre-concentration liquid into ion exchange resin and carries out desalination, obtains seeing through liquid, and described ion exchange resin refers to the mixed bed of anion-cation exchange resin;
Step 5, sends into vaporizer by step 4 gained through liquid concentrated, obtains sucrose concentrated solution;
Step 6, when step 5 gained sucrose concentrated solution is warming up to supersaturation, adds crystal seed, and natural decrease temperature crystalline is incubated to crystallization completely in Tc, by centrifugal gained crystallization, obtain yellow gold sugar crystal;
Step 7, step 6 gained yellow gold sugar crystal is dry, obtain finished product.
First pass through draining device, sugarcane or beet are squeezed, obtain sucrose mix juice, then sucrose mix juice is carried out to pre-treatment through coarse filter, remove larger bagasse or beet pulp, to be applied to better follow-up membrane sepn operation, coarse filter herein includes but are not limited to: deep bed filter or screen cloth (aperture of screen cloth is preferably 100～200 orders) etc., fully to remove bagasse or beet pulp.The effect of microfiltration membrane is some granule foreigns, the colloid etc. of removing in sucrose mix juice, can improve purity and the quality of product.Pre-concentration is removed a part of impurity in sucrose mix juice clear liquid and pigment, can not only improve product quality, can also extend the life-span of ion exchange resin.Ion exchange resin can be removed in pre-concentration liquid with salinity and partial pigment, further improves purity and the quality of product.
In step 2, microfiltration membrane preferably adopts ceramic microfiltration membrane or the organic microfiltration membrane of tubular type, and in order to make filter effect more excellent, the mean pore size scope of the microfiltration membrane of employing is 50～500nm.If mean pore size is too little, can cause filtration flux too little, and the sucrose of a part of larger particles can be trapped, have influence on yield; If mean pore size is too large, can cause a part of impurity and pigment to see through rete and enter to per-meate side, have influence on the colour of product.On this basis, the film that mean pore size is 200nm is held back some fat, the protein got rid of in sucrose, and this can ensure the life of ion exchange resin, and can prevent that resin from, by macromole impurity absorption, having influence on the decreasing ratio for salt.Filtration temperature exerts an influence for product quality and strainability, although filtration temperature improves viscosity, the raising filtration flux that can reduce filtered liquid, if but filtration temperature is too high, can there is sex change in some materials in sucrose mix juice, have influence on the quality of the finished product, preferably 20～90 DEG C of filtration temperatures, more excellent is 80 DEG C, in the time that filtering, this temperature section can ensure that filtration flux declines slowly, superior product quality simultaneously.If when filter pressure is less than normal, can cause flux low, do not conform to and be suitable for engineering actual demand, if when pressure is excessive, can cause a part of most of impurity to be pressed, see through rete, cause product colour bad, and can produce more serious Pore Blocking, and make it be difficult for being cleaned, preferred filter pressure is 0.1～0.5MPa; Optimum is 0.3MPa, can ensure that filtration flux declines slowly simultaneously.
In step 3, what pre-concentration preferably adopted is 2nd effect evaporator or nanofiltration membrane.If produce steam as the energy taking burning bagasse, can select pre-concentration device is 2nd effect evaporator, and the sucrose mix juice in step 2 is concentrated to 40%, and the cost of one ton of water of every like this evaporation is only 6-8 unit, can reduce production costs; If taking fire coal as the energy, carry out pre-concentration by nanofiltration membrane.
Preferably, pre-concentration adopts nanofiltration membrane, and nanofiltration meeting sees through part ion, and these ions, in follow-up ion exchange process, have influence on decolorizing effect, cause colour bigger than normal.When the molecular weight cut-off of nanofiltration membrane is excessive, can cause sucrose to see through rete, yield is reduced, if when molecular weight cut-off is too small, can cause filtration flux little, can not reach suitable cycles of concentration, make subsequent evaporation process energy consumption bigger than normal, preferably molecular weight cut-off is 100～500Da; More preferably 150Da, can ensure that membrane flux is higher, film pollutes slowly, and film is very high to the rejection of sucrose simultaneously, and the yield of sucrose is more than 99.9%.In this step, preferably the volume of sucrose mix juice clear liquid is concentrated into 30%～40%, cycles of concentration is higher, can ensure that the input concentration of subsequent processing section ion exchange resin is higher, enhances productivity; Slough on the other hand 2/3 water, can save larger energy consumption, also removed 60% salinity simultaneously.When the pressure of nanofiltration is too small, can cause that flux is little, cycles of concentration cannot get a promotion, if pressure is excessive, can cause the decline of the rejection of some sucrose, and can cause cake layer to be compacted, have influence on flux and film and clean, preferably 1.0～4.0Mpa, optimum is 3.0MPa, can ensure that average filtration flux is larger, can reach 20L/m
2h, can effectively enhance productivity like this.The material of nanofiltration membrane is also to need through preferred, due to when the nanofiltration separation, have sieve effect and electrocharge effect simultaneously, ensure highly to the decreasing ratio of salt and high to the rejection of sucrose simultaneously, optimum is the nanofiltration membrane that adopts ceramic material, polyethersulfone or polyamide-based material.
In step 4, ion exchange resin is to be the mixed bed of anion-cation exchange resin, and described ion exchange resin adsorption tower blade diameter length ratio is 1/2～1/10, and flow velocity is 1～10BV/h, and temperature is 20～80 DEG C.In addition, be 1/3 at adsorption tower blade diameter length ratio, flow velocity is 4BV/h, and when temperature is 55 DEG C, the best results of desalination and decolouring, can slough 98% salinity, and simultaneously the yield of sucrose is 99.6%, colour is at 2500IU.
In step 5, preferably adopt MVR evaporation equipment or multifunctional evaporating equipment, thickening temperature is 30-60 DEG C.This MVR evaporation equipment can be larger reduction energy consumption, can save more than 60% evaporation energy consumption.
In step 6, in step 6, sucrose concentrated solution is warming up to 70 DEG C, is 1.05 o'clock until the degree of supersaturation of syrup, start naturally cooling decrease temperature crystalline, while cooling the temperature to 50 DEG C, keep 50 DEG C of crystallizations, collect crystallization, by centrifugal gained crystallization.
Based on above-mentioned method, another object of the present invention has been to provide a kind of production equipment of yellow gold sugar, includes the coarse filter, microporous filtration, nano-filtration membrane filter, anion-cation exchange resin bed, the vaporizer that connect successively.
Described coarse filter is sand filtering device, deep bed filter, filter cloth or screen cloth.
The material of described nanofiltration membrane is pottery, polyethersulfone or polymeric amide, and the molecular weight cut-off of nanofiltration membrane is 150Da.
Yellow gold sugar production method provided by the invention can be directly taking sugarcane or beet as raw material, continuously produce high-quality gold sugar, the colourimetric number of products obtained therefrom 800～3000, ratio of desalinization is high, yield is high.
Brief description of the drawings
Fig. 1 is the technological process of production schematic diagram of the yellow gold sugar that the present invention relates to;
Fig. 2 is the production equipment schematic diagram of the yellow gold sugar that the present invention relates to.
Embodiment
Embodiment 1
As shown in Figure 1, the novel process of a kind of direct-edible syrup of the present invention comprises the following steps:
Squeeze the juice: sugarcane is squeezed by draining device, obtain sugar cane juice;
Pre-filtering, is undertaken gained sugar cane juice after pre-filtering by screen cloth, removes larger bagasse, and the aperture of screen cloth is 100 orders;
Micro-filtrate membrane filtration: the sugar cane juice that pre-filtering is collected, by 500nm microfiltration of ceramic membrane, feed temperature is 20 DEG C, and filter pressure is 0.5Mpa, obtains sugar cane juice clear liquid, and sucrose concentration is 12%; ;
Membrane concentration: sugar cane juice clear liquid enters nano-filtration membrane filter and concentrates, nanofiltration membrane material is polyethersulfone, and molecular weight cut-off is 100Da, and nanofiltration pressure 4.0Mpa, is concentrated into 30% by the volume of sugar cane juice clear liquid;
Ion-exchange desalination: the sugar cane juice after concentrated is carried out to desalination and decolouring with anion-cation exchange resin bed, and blade diameter length ratio is 1/7, and flow velocity is 4BV/h, and temperature is 30 DEG C; Anion-cation exchange resin mixed bed is to be mixed and fill by weight 1:1 by anionite-exchange resin D202 and Zeo-karb 732.
Concentrated: the sugar cane juice after desalination is sent into MVR vaporizer, and thickening temperature is 60 DEG C, obtains sucrose concentrated solution, and the mass concentration of sucrose concentrated solution is 60%;
Crystallization: sucrose concentrated solution is warming up to 70 DEG C, is 1.05 o'clock until the degree of supersaturation of syrup, start naturally cooling decrease temperature crystalline, while cooling the temperature to 50 DEG C, collect crystallization, by centrifugal gained crystallization, obtain yellow gold sugar crystal;
Dry: by the forced air drying of gained yellow gold sugar crystal, to obtain finished product.
After testing, the present embodiment gained finished product pigment removal is 93%, and salinity clearance is 92%, sucrose is divided into 99.3%, and it is 0.02% that electricity is led ash content, and colour is 1200IU, water insoluble impurity 12mg/kg, the sucrose rate of recovery is 95.4%, ion exchange resin regeneration frequency is about every 12 batches.
Embodiment 2
The difference of the present embodiment and embodiment 1 is: lack the step of micro-filtration, detailed process is as follows:
Squeeze the juice: sugarcane is squeezed by draining device, obtain sugar cane juice;
Pre-filtering, is undertaken gained sugar cane juice after pre-filtering by screen cloth, removes larger bagasse, and the aperture of screen cloth is 100 orders;
Membrane concentration: sugar cane juice clear liquid enters nano-filtration membrane filter and concentrates, nanofiltration membrane material is polyethersulfone, and molecular weight cut-off is 100Da, and nanofiltration pressure 4.0Mpa, is concentrated into 30% by the volume of sugar cane juice clear liquid;
Ion-exchange desalination: the sugar cane juice after concentrated is carried out to desalination and decolouring with anion-cation exchange resin bed, and blade diameter length ratio is 1/7, and flow velocity is 4BV/h, and temperature is 30 DEG C; Anion-cation exchange resin mixed bed is to be mixed and fill by weight 1:1 by anionite-exchange resin D202 and Zeo-karb 732.
Concentrated: the sugar cane juice after desalination is sent into MVR vaporizer, and thickening temperature is 60 DEG C, obtains sucrose concentrated solution, and the mass concentration of sucrose concentrated solution is 60%;
Crystallization: sucrose concentrated solution is warming up to 70 DEG C, is 1.05 o'clock until the degree of supersaturation of syrup, start naturally cooling decrease temperature crystalline, while cooling the temperature to 50 DEG C, collect crystallization, by centrifugal gained crystallization, obtain yellow gold sugar crystal;
Dry: by the forced air drying of gained yellow gold sugar crystal, to obtain finished product.
After testing, the present embodiment gained finished product pigment removal is 87%, and salinity clearance is 85%, and sucrose is divided into 98.4%, and it is 0.15% that electricity is led ash content, and colour is 800IU, and the sucrose rate of recovery is 91.2%, and regeneration of ion-exchange resin frequency is about every 5 batches.
Yield and the quality of embodiment 1 finished product are all better than the present embodiment finished product, this may be because micro-filtration step can be held back some impurity and the colloid in sucrose, thereby have influence on follow-up nanofiltration and resin absorption process, nanofiltration meeting sees through more polyion, make resin easily by contaminating impurity, cause removing salt and pigment, and shorten resin work-ing life.
Embodiment 3
The difference of the present embodiment and embodiment 1 is: what concentration technology adopted is 2nd effect evaporator, and detailed process is as follows:
Squeeze the juice: sugarcane is squeezed by draining device, obtain sugar cane juice;
Pre-filtering, is undertaken gained sugar cane juice after pre-filtering by screen cloth, removes larger bagasse, and the aperture of screen cloth is 100 orders;
Micro-filtrate membrane filtration: the sugar cane juice that pre-filtering is collected, by 500nm microfiltration of ceramic membrane, feed temperature is 20 DEG C, and filter pressure is 0.5Mpa, obtains sugar cane juice clear liquid, and sucrose concentration is 12%; ;
Membrane concentration: sugar cane juice clear liquid enters 2nd effect evaporator and concentrates, is concentrated into 30% by the volume of sugar cane juice clear liquid;
Ion-exchange desalination: the sugar cane juice after concentrated is carried out to desalination and decolouring with anion-cation exchange resin bed, and blade diameter length ratio is 1/7, and flow velocity is 4BV/h, and temperature is 30 DEG C; Anion-cation exchange resin mixed bed is to be mixed and fill by weight 1:1 by anionite-exchange resin D202 and Zeo-karb 732.
Concentrated: the sugar cane juice after desalination is sent into MVR vaporizer, and thickening temperature is 60 DEG C, obtains sucrose concentrated solution, and the mass concentration of sucrose concentrated solution is 60%;
Crystallization: sucrose concentrated solution is warming up to 70 DEG C, is 1.05 o'clock until the degree of supersaturation of syrup, start naturally cooling decrease temperature crystalline, while cooling the temperature to 50 DEG C, collect crystallization, by centrifugal gained crystallization, obtain yellow gold sugar crystal;
Dry: by the forced air drying of gained yellow gold sugar crystal, to obtain finished product.
After testing, embodiment gained finished product pigment removal is 90%, and salinity clearance is 87%, and sucrose is divided into 97.3%, and it is 0.17% that electricity is led ash content, and colour is 750IU, and the sucrose rate of recovery is 93.5%, and regeneration of ion-exchange resin frequency is about every 8 batches.
Yield and the quality of embodiment 1 finished product are all better than the present embodiment finished product, illustrate that nanofiltration membrane is with respect to 2nd effect evaporator, there is the effect of improving the quality of products, this may be because nanofiltration meeting sees through part ion, these ions are in follow-up ion exchange process, have influence on decolorizing effect, cause colour bigger than normal.
Embodiment 4
As shown in Figure 1, the novel process of a kind of direct-edible syrup of the present invention comprises the following steps:
Squeeze the juice: sugarcane is squeezed by draining device, obtain sugar cane juice;
Pre-filtering, walks gained sugar cane juice to carry out after pre-filtering by filter, removes larger bagasse, and the aperture of screen cloth is 100 orders;
Micro-filtrate membrane filtration: the sugar cane juice that pre-filtering is collected, by 200nm tubular type ceramic microfiltration membrane, feed temperature is 80 DEG C, and filter pressure is 0.3Mpa, obtains sugar cane juice clear liquid, and sucrose concentration is 18%; ;
Membrane concentration: sugar cane juice clear liquid enters nano-filtration membrane filter and concentrates, nanofiltration membrane material is polyethersulfone, molecular weight cut-off is respectively 100Da, 150Da, 200Da, 300Da, 400Da, 500Da, and nanofiltration pressure 3.0Mpa, is concentrated into 40% by the volume of sugar cane juice clear liquid;
Ion-exchange desalination: the sugar cane juice after concentrated is carried out to desalination and decolouring with anion-cation exchange resin bed, and blade diameter length ratio is 1/3, and flow velocity is 10BV/h, and temperature is 55 DEG C; Anion-cation exchange resin mixed bed is to be mixed and fill by weight 1:1 by anionite-exchange resin D202 and Zeo-karb 732.
Concentrated: the sugar cane juice after desalination is sent into MVR vaporizer, and thickening temperature is 60 DEG C, obtains sucrose concentrated solution, and the mass concentration of sucrose concentrated solution is 70%;
Crystallization: sucrose concentrated solution is warming up to 70 DEG C, is 1.05 o'clock until the degree of supersaturation of syrup, start naturally cooling decrease temperature crystalline, while cooling the temperature to 50 DEG C, collect crystallization, by centrifugal gained crystallization, obtain yellow gold sugar crystal;
Dry: by the forced air drying of gained yellow gold sugar crystal, to obtain finished product.
Gained finished product is detected, and result is as follows:
| ? | Batch 1 | Batches 2 | Batches 3 | Batches 4 | Batches 5 | Batches 6 |
| Nanofiltration membrane molecular weight cut-off | 100 | 150 | 200 | 300 | 400 | 500 |
| Pigment removal | 93％ | 99％ | 92％ | 95％ | 94％ | 91％ |
| Salinity clearance | 92％ | 99％ | 91％ | 90％ | 89％ | 93％ |
| Sucrose | 98.5％ | 99.8％ | 98.6％ | 98.5％ | 98.5％ | 98.7％ |
| Electricity is led ash content | 0.04％ | 0.01％ | 0.06％ | 0.08％ | 0.07％ | 0.09％ |
| Colour | 800IU | 2400IU | 1200IU | 1000IU | 1500IU | 1800IU |
| The sucrose rate of recovery | 92.5％ | 99.9％ | 97.4％ | 95.3％ | 96.1％ | 94.2％ |
| Ion exchange resin regeneration frequency | Approximately every 12 batches | The approximately the 15th batch | Approximately every 8 batches | Approximately every 10 batches | Approximately every 9 batches | Approximately every 11 batches |
As can be seen from the above table, when the molecular weight cut-off of nanofiltration membrane is excessive, can cause sucrose to see through rete, yield is reduced, if when molecular weight cut-off is too small, can cause filtration flux little, can not reach suitable cycles of concentration, make subsequent evaporation process energy consumption bigger than normal, more preferably 150Da, these processing condition are optimum embodiment of the present invention, can ensure that membrane flux is higher, film pollutes slowly, film is very high to the rejection of sucrose simultaneously, and the yield of sucrose is more than 99.9%, and colour reaches 2400IU.
Embodiment 5
As shown in Figure 1, the novel process of a kind of direct-edible syrup of the present invention comprises the following steps:
Squeeze the juice: sugarcane is squeezed by draining device, obtain sugar cane juice;
Pre-filtering, walks gained sugar cane juice to carry out after pre-filtering by filter, removes larger bagasse, and the aperture of screen cloth is 100 orders;
Micro-filtrate membrane filtration: the sugar cane juice that pre-filtering is collected, by 200nm tubular type organic membrane micro-filtration, feed temperature is 50 DEG C, and filter pressure is 0.3Mpa, obtains sugar cane juice clear liquid, and sucrose concentration is 20%; ;
Membrane concentration: sugar cane juice clear liquid enters nano-filtration membrane filter and concentrates, nanofiltration membrane material is polyethersulfone, and molecular weight cut-off is 150Da, and nanofiltration pressure 3.0Mpa, by the volume of sugar cane juice clear liquid simmer down to 10%, 20%, 30%, 40%, 50% respectively;
Ion-exchange desalination: the sugar cane juice after concentrated is carried out to desalination and decolouring with anion-cation exchange resin bed, and blade diameter length ratio is 1/3, and flow velocity is 4BV/h, and temperature is 55 DEG C; Anion-cation exchange resin mixed bed is to be mixed and fill by weight 1:1 by anionite-exchange resin D202 and Zeo-karb 732.
Concentrated: the sugar cane juice after desalination is sent into MVR vaporizer, and thickening temperature is 60 DEG C, obtains sucrose concentrated solution, and the mass concentration of sucrose concentrated solution is 70%;
Crystallization: sucrose concentrated solution is warming up to 70 DEG C, is 1.05 o'clock until the degree of supersaturation of syrup, start naturally cooling decrease temperature crystalline, while cooling the temperature to 50 DEG C, collect crystallization, by centrifugal gained crystallization, obtain yellow gold sugar crystal;
Dry: by the forced air drying of gained yellow gold sugar crystal, to obtain finished product.
Gained finished product is detected, and result is as follows:
| ? | Batch 1 | Batches 2 | Batches 3 | Batches 4 | Batches 5 |
| Cycles of concentration | 10％ | 20％ | 30％ | 40％ | 50％ |
| Pigment removal | 86％ | 91％ | 92％ | 97.5％ | 84％ |
| Salinity clearance | 85％ | 86％ | 90％ | 98.0％ | 92％ |
| Sucrose | 915％ | 92.2％ | 95.6％ | 99.5％ | 94.1％ |
| Electricity is led ash content | 0.08％ | 0.06％ | 0.03％ | 0.02％ | 0.12％ |
| Colour | 300IU | 600IU | 3000IU | 2500IU | 10000IU |
| The sucrose rate of recovery | 86.5％ | 90.0％ | 91.2％ | 99.0％ | 93.1％ |
| Ion exchange resin regeneration frequency | Approximately every 12 batches | The approximately the 15th batch | Approximately every 8 batches | Approximately every 10 batches | Approximately every 9 batches |
As can be seen from the above table, when cycles of concentration is promoted to 50% from 10%, under too low cycles of concentration condition, because the concentration of concentrated solution is too low, in the process process of resin absorption, can cause resin also can adsorb more coloring matter, make the colour in product on the low side, lower than the lower value of yellow gold sugar examination criteria; And, if cycles of concentration is too low, can cause, in the process of desalination, wash-out, having more salinity by wash-out out, cause in finished product ash content higher.If when cycles of concentration is too high, from also finding out, can cause the colour of product to exceed standard value, and can cause salinity clearance and product ash content higher.
Claims (10)
1. a production technique for yellow gold sugar, is characterized in that: comprise the following steps:
Step 1, squeezes sugarcane or beet by draining device, obtain sucrose mix juice;
Step 2, is undertaken step 1 gained sucrose mix juice after pre-filtering by coarse filter, then sends into microfiltration membrane and filter, and obtains sucrose mix juice clear liquid;
Step 3, carries out pre-concentration by step 2 gained sucrose mix juice clear liquid, makes the volume of sucrose mix juice clear liquid be concentrated into 30%～40%, obtains pre-concentration liquid;
Step 4, sends step 3 gained pre-concentration liquid into ion exchange resin and carries out desalination, obtains seeing through liquid, and described ion exchange resin refers to anion-cation exchange resin bed;
Step 5, sends into vaporizer by step 4 gained through liquid concentrated, obtains sucrose concentrated solution;
Step 6, when step 5 gained sucrose concentrated solution is warming up to supersaturation, adds crystal seed, and natural decrease temperature crystalline is incubated to crystallization completely in Tc, by centrifugal gained crystallization, obtain yellow gold sugar crystal;
Step 7, step 6 gained yellow gold sugar crystal is dry, obtain finished product.
2. the production technique of yellow gold sugar according to claim 1, it is characterized in that: the microfiltration membrane in step 2 adopts ceramic microfiltration membrane or the organic microfiltration membrane of tubular type, mean pore size scope is 50～500 nm, and the pressure range of micro-filtration is 0.1～0.5MPa, 20～90 DEG C of feed temperatures in microfiltration process.
3. the production technique of yellow gold sugar according to claim 1, is characterized in that: in step 3, adopt 2nd effect evaporator or nanofiltration membrane to carry out pre-concentration.
4. the production technique of yellow gold sugar according to claim 3, is characterized in that: the material of described nanofiltration membrane is pottery, polyethersulfone or polymeric amide, and the molecular weight cut-off of nanofiltration membrane is 100～500Da, and the pressure range of nanofiltration is 1.0～4.0Mpa.
5. the production technique of yellow gold sugar according to claim 1, is characterized in that: step 4 intermediate ion exchange resin adsorption tower blade diameter length ratio is 1/2～1/10, and flow velocity is 1～10BV/h, and temperature is 20～80 DEG C.
6. the production technique of yellow gold sugar according to claim 1, is characterized in that: in step 5, adopt MVR evaporation equipment or multifunctional evaporating equipment, thickening temperature is 30～60 DEG C.
7. the production technique of yellow gold sugar according to claim 1, is characterized in that: in step 6, sucrose concentrated solution is warming up to 70 DEG C, is 1.05 o'clock until the degree of supersaturation of syrup, start naturally cooling decrease temperature crystalline, while cooling the temperature to 50 DEG C, keep 50 DEG C of crystallizations.
8. a production equipment for yellow gold sugar, is characterized in that: include the coarse filter, microporous filtration, nano-filtration membrane filter, anion-cation exchange resin bed, the vaporizer that connect successively.
9. yellow gold sugar production equipment according to claim 8, is characterized in that: described coarse filter is sand filtering device, deep bed filter, filter cloth or screen cloth.
10. yellow gold sugar production equipment according to claim 8, is characterized in that: the material of described nanofiltration membrane is pottery, polyethersulfone or polymeric amide, and the molecular weight cut-off of nanofiltration membrane is 150Da.
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| CN104805224A (en) * | 2015-04-02 | 2015-07-29 | 广西大学 | Originally ecological black sugar processing device |
| CN104805222A (en) * | 2015-04-02 | 2015-07-29 | 广西大学 | Refined sugar clarification device |
| CN104805228A (en) * | 2015-04-02 | 2015-07-29 | 广西大学 | Sugar juice evaporation method |
| CN105420419A (en) * | 2015-12-10 | 2016-03-23 | 中粮集团有限公司 | Method for purifying and concentrating beet sugar manufacture clarified juice and sugar making method adopting method for purifying and concentrating beet sugar manufacture clarified juice |
| WO2017049745A1 (en) * | 2015-09-21 | 2017-03-30 | 江苏久吾高科技股份有限公司 | Membrane separation production method and device for edible raw sugar |
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| CN104805225A (en) * | 2015-04-02 | 2015-07-29 | 广西大学 | Originally ecological black sugar processing method |
| CN104805224A (en) * | 2015-04-02 | 2015-07-29 | 广西大学 | Originally ecological black sugar processing device |
| CN104805222A (en) * | 2015-04-02 | 2015-07-29 | 广西大学 | Refined sugar clarification device |
| CN104805228A (en) * | 2015-04-02 | 2015-07-29 | 广西大学 | Sugar juice evaporation method |
| CN104805222B (en) * | 2015-04-02 | 2018-02-27 | 广西大学 | A kind of refined sugar clarifier |
| CN104805225B (en) * | 2015-04-02 | 2018-02-27 | 广西大学 | A kind of processing method of ecosystem brown sugar |
| WO2017049745A1 (en) * | 2015-09-21 | 2017-03-30 | 江苏久吾高科技股份有限公司 | Membrane separation production method and device for edible raw sugar |
| CN105420419A (en) * | 2015-12-10 | 2016-03-23 | 中粮集团有限公司 | Method for purifying and concentrating beet sugar manufacture clarified juice and sugar making method adopting method for purifying and concentrating beet sugar manufacture clarified juice |
| CN107142336A (en) * | 2017-05-08 | 2017-09-08 | 丁宁 | The sugar-free brown sugar preparation method and applications of sucrose in brown sugar are sloughed in a kind of nanofiltration |
| CN110016525A (en) * | 2019-04-10 | 2019-07-16 | 中国科学院近代物理研究所 | A kind of functional food sugar grass syrup and preparation method thereof |
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