WO2017071585A1 - Appareil et procédé pour la récupération de sucre résiduel dans un processus de production de sucre de canne - Google Patents

Appareil et procédé pour la récupération de sucre résiduel dans un processus de production de sucre de canne Download PDF

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WO2017071585A1
WO2017071585A1 PCT/CN2016/103398 CN2016103398W WO2017071585A1 WO 2017071585 A1 WO2017071585 A1 WO 2017071585A1 CN 2016103398 W CN2016103398 W CN 2016103398W WO 2017071585 A1 WO2017071585 A1 WO 2017071585A1
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membrane module
stage
ultrafiltration
nanofiltration
sugar
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PCT/CN2016/103398
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English (en)
Chinese (zh)
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万印华
罗建泉
杭晓风
陈向荣
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中国科学院过程工程研究所
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Priority to AU2016347128A priority Critical patent/AU2016347128B2/en
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    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
    • C13B20/00—Purification of sugar juices
    • C13B20/16—Purification of sugar juices by physical means, e.g. osmosis or filtration

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  • the invention belongs to the technical field of sugar production, and relates to a device and a method for recovering residual sugar in sugar cane sugar-making process, in particular to a device and a method for recovering residual sugar in sugar cane sugar-making process by multi-stage countercurrent washing and filtering method.
  • the existing sugar cane sugar production process includes pretreatment of sugar cane, juice extraction, clarification of cane juice, and scouring.
  • the clarification effect of the cane juice directly determines the quality of the finished sugar.
  • the traditional process is to add a large amount of lime and sulfur dioxide (sulfuric acid method) to the mixed juice, or add lime and carbonic acid gas (carbonic acid).
  • the method then separates the precipitate to remove non-sugar impurities in the mixed juice to reduce chroma and turbidity. Therefore, a large amount of waste water and solid waste are generated in the sugar-making process, and there are problems such as complicated process, low decolorization rate, and unstable quality of the finished sugar.
  • the domestic sugar cane factory especially the sulphuric acid sugar factory, often affects the quality of the product due to the exceeding of the standard values of color value and turbidity, and even causes the product to be degraded or become an external sugar.
  • CN 103194545B discloses a method for treating sugarcane mixed juice by membrane method, the method comprising the following steps: (1) mixing the clear juice into the first-stage ultrafiltration membrane, filtering the obtained supernatant and then entering the second-stage ultrafiltration membrane.
  • the concentrated solution filtered by the first-stage ultrafiltration membrane is evaporated to sugar, and the concentrated solution filtered by the second-stage ultrafiltration membrane is combined with the mixed clear juice to be filtered into the first-stage ultrafiltration membrane; (2) in step (1)
  • the fresh liquid obtained by filtering the second-stage ultrafiltration membrane enters the membrane concentrating device and is concentrated to obtain a concentrate and fresh water;
  • the first-stage ultrafiltration membrane has a molecular weight cut off of 50,000 to 100,000 Daltons, and the second The ultrafiltration membrane has a molecular weight cutoff of from 1,000 to 20,000 Daltons.
  • This method includes two-stage ultrafiltration clarification decolorization and first-stage reverse osmosis concentration dehydration, but due to ultrafiltration, there is a certain retention of sucrose.
  • the two-stage ultrafiltration concentrate contains a high concentration of sucrose, and the recovery rate of sucrose is generally only 60-70%, thereby causing a large loss of residual sugar.
  • Both CN102659855A and CN103710470A disclose methods for achieving decolorization of sugar juice by combining membrane separation with ion exchange, but none of the problems of recovery of residual sugar in concentrate or elution concentrate are mentioned.
  • CN 201510486534.4 The concentrated liquid in the decolorization section is treated by adding chemicals such as lime or sulfur dioxide to return to the clarification section, but the process still does not get rid of the traditional chemical method, causing the contamination of the molasses to decrease the added value.
  • the washing process is a key technology in the membrane separation process, mainly used for desalination and improving product purity.
  • the washing operation includes an equal volume continuous washing and a dilution-concentration variable volume intermittent washing.
  • the former has high filtration efficiency and is easy to operate continuously; the latter has a large filtration flux, but consumes a large amount of water and requires an additional buffer tank.
  • the present invention aims to provide a device and a method for recovering residual sugar in a sugar cane sugar-making process, which not only can recover most of the residual sugar in the sucrose refining process, but also reduce the washing and filtering.
  • the water consumption is small, and the device is simple and safe to operate, easy to produce continuously, and the obtained sugar-containing concentrate has no chemical additive.
  • One of the objects of the present invention is to provide a device for recovering residual sugar in a sugar cane sugar-making process, the device comprising a multi-stage countercurrent washing unit and a nanofiltration concentration unit, the multi-stage countercurrent washing unit comprising at least 2 levels of super a membrane module, the nanofiltration concentration unit comprising a nanofiltration membrane module;
  • the intercepting side outlet of the pre-stage ultrafiltration membrane module of the multi-stage countercurrent washing unit is connected to the intercepting side inlet of the latter-stage ultrafiltration membrane module, and the intercepting side inlet and the latter stage of the pre-stage ultrafiltration membrane module are super The permeate side outlets of the membrane module are connected;
  • the cut-off side of the nanofiltration membrane module results in a sugar-containing concentrate, and the retentate side of the last stage ultrafiltration membrane module of the multi-stage countercurrent washing unit obtains a retentate.
  • the device is mainly used for recovering residual sugar in the process of sugar production by membrane method, and can also be used for recovery of residual sugar in other methods of sugar production.
  • the recovery device uses multi-stage countercurrent washing technology to separate the sucrose and non-sugar substances in the residual sugar solution, reduce the residual sugar loss in the sucrose refining process, and improve the recovery rate of sucrose in the whole clarification decolorization section, thereby reducing Sucrose production costs.
  • the permeate side outlet of the nanofiltration membrane module is connected to the intercepting side inlet of the last stage ultrafiltration membrane module of the multistage countercurrent washing unit, thereby realizing the recycling of water and greatly saving the washing water.
  • the washing mode of the multi-stage countercurrent washing unit is an equal volume countercurrent washing.
  • the equal volume countercurrent washing is continuously pumping the washing water into the final stage ultrafiltration membrane module, and controlling the water addition rate to be equal to the permeate membrane flux of the ultrafiltration membrane module, so as to maintain the volume of the washing residue at each level. constant.
  • the multi-stage countercurrent washing unit is used for removing macromolecular impurities in a sugar-containing solution, and the multi-stage countercurrent washing unit comprises a 2-5-stage ultrafiltration membrane module, such as a 2-stage ultrafiltration membrane module, and a 3-stage. Ultrafiltration membrane module, 4-stage ultrafiltration membrane module or 5-stage ultrafiltration membrane module.
  • the ultrafiltration membrane module has a molecular weight cut off of 1000-5000 Da, such as 1500 Da, 2000 Da, 2500 Da, 3000 Da, 3500 Da, 4000 Da or 4500 Da, and the like.
  • the ultrafiltration membrane module has an operating temperature of 25-95 ° C, such as 30 ° C, 40 ° C, 50 ° C, 60 ° C, 65 ° C, 70 ° C, 80 ° C, 90 ° C or 95 ° C, and the like.
  • the operating pressure of the ultrafiltration membrane module is 0.5-1.5 MPa, such as 0.6 MPa, 0.8 MPa, 1.0 MPa, 1.2 MPa, 1.3 MPa or 1.4 MPa, and the like.
  • the ultrafiltration membrane module is in the form of a coil, a tube, a plate or a hollow fiber.
  • the material of the ultrafiltration membrane module is polysulfone, polyethersulfone, sulfonated polyethersulfone or polyvinylidene fluoride.
  • the ultrafiltration membrane modules of the multi-stage countercurrent washing unit may be composed of one or more ultrafiltration membrane modules connected in parallel, such as two, three, four, six or eight parallel ultrafiltrations.
  • Membrane assembly composition one skilled in the art can select the appropriate number of ultrafiltration membrane modules based on the actual flow rate.
  • the nanofiltration concentration unit is for further concentrating the sugar-containing solution obtained by the multi-stage countercurrent washing unit, and the nanofiltration membrane module is in the form of a roll membrane.
  • the nanofiltration membrane module may be composed of one or more nanofiltration membrane modules in parallel, such as two, three, four, six or eight parallel nanofiltration membrane modules, which can be used by those skilled in the art. Select the appropriate number of nanofiltration membrane modules based on the actual flow rate.
  • the nanofiltration membrane module has a membrane molecular weight cutoff of from 90 to 400 Da, such as 100 Da, 120 Da, 150 Da, 200 Da, 250 Da, 300 Da or 350 Da, etc., preferably 200 Da.
  • the nanofiltration membrane module has an operating temperature of 25-95 ° C, such as 30 ° C, 40 ° C, 50 ° C, 60 ° C, 70 ° C, 80 ° C or 90 ° C, and the like.
  • the nanofiltration membrane module has an operating pressure of 2.0 to 4.1 MPa, such as 2.2 MPa, 2.5 MPa, 2.8 MPa, 3.0 MPa, 3.2 MPa, 3.5 MPa, 3.8 MPa or 4.0 MPa, and the like.
  • Another object of the present invention is to provide a method for recovering residual sugar using the apparatus as described above, the method comprising the steps of:
  • the first-stage ultrafiltration permeate is subjected to nanofiltration to concentrate to obtain a sugar-containing concentrate and a nanofiltration permeate.
  • the residual sugar recovery method provided by the invention can be used as the washing water for the upper stage of the washing liquid produced by each stage of washing, and the first stage washing and filtering liquid has a high sugar concentration and directly enters the nanofiltration concentrated section.
  • Production wash The water is filtered, which greatly saves water consumption, reduces the energy consumption of the nanofiltration concentration and evaporation crystallization section, and is easy to continuously produce without chemical additives.
  • the sugar-containing solution in the step (1) is a concentrated solution of the sugar cane mixed juice after microfiltration pretreatment and ultrafiltration decolorization treatment 10-30 times, such as concentration 12 times, 15 times, 20 times, 22 times, 25 times or Concentrate after 28 times.
  • the multi-stage countercurrent ultrafiltration in the step (1) is an equal volume countercurrent washing.
  • the washing water for the multi-stage countercurrent ultrafiltration in the step (1) is deionized water.
  • the washing water volume of the multi-stage countercurrent washing unit described in the step (1) is 1-3 times, such as 1 time, 2 times or 3 times, of the volume of the sugar-containing solution.
  • the last stage ultrafiltration retentate of step (1) is used to extract natural pigments.
  • Step (1) The multi-stage countercurrent ultrafiltration is carried out through a 2-5 ultrafiltration membrane module, such as by including a 2-stage ultrafiltration membrane module, a 3-stage ultrafiltration membrane module, a 4-stage ultrafiltration membrane module, or a 5-stage ultrafiltration unit.
  • the membrane module is subjected to countercurrent ultrafiltration.
  • the ultrafiltration membrane module has a molecular weight cut off of 1000-5000 Da, such as 1500 Da, 2000 Da, 2500 Da, 3000 Da, 3500 Da, 4000 Da or 4500 Da, and the like.
  • the ultrafiltration membrane module has an operating temperature of 25-95 ° C, such as 30 ° C, 40 ° C, 50 ° C, 60 ° C, 65 ° C, 70 ° C, 80 ° C, 90 ° C or 95 ° C, and the like.
  • the ultrafiltration membrane module has an operating pressure of 0.5-1.5 MPa, such as 0.6 MPa, 0.8 MPa, 1.0 MPa, 1.2 MPa, 1.3 MPa, or 1.4 MPa, and the like.
  • the ultrafiltration membrane module is in the form of a coil, a tube, a plate or a hollow fiber.
  • the material of the ultrafiltration membrane module is polysulfone, polyethersulfone, sulfonated polyethersulfone or polyvinylidene fluoride.
  • step (2) The nanofiltration concentration of step (2) is carried out through a nanofiltration membrane module.
  • the nanofiltration membrane module has a molecular weight cut-off of 90-400 Da, such as 100 Da, 120 Da, 150Da, 200Da, 250Da, 300Da or 350Da, etc., preferably 200Da.
  • the nanofiltration membrane module has an operating temperature of 25-95 ° C, such as 30 ° C, 40 ° C, 50 ° C, 60 ° C, 70 ° C, 80 ° C or 90 ° C, and the like.
  • the nanofiltration membrane module has an operating pressure of 2.0 to 4.1 MPa, such as 2.2 MPa, 2.5 MPa, 2.8 MPa, 3.0 MPa, 3.2 MPa, 3.5 MPa, 3.8 MPa or 4.0 MPa, and the like.
  • the nanofiltration membrane module is in the form of a roll film.
  • the sugar-containing concentrate of step (2) is crystallized by evaporation to obtain a sugar.
  • the nanofiltration permeate of the step (2) is used as the washing water for the multistage countercurrent ultrafiltration of the step (1).
  • the volume ratio of the nanofiltration permeate in the step (2) to the washing water used in the multistage countercurrent ultrafiltration in the step (1) is 2:3 to 1:5, such as 4:15, 1:3. , 7:15 or 3:5, etc.
  • the nanofiltration permeate is used as the washing water for multi-stage countercurrent ultrafiltration, which can greatly save water consumption.
  • the method for recovering residual sugar includes the following steps:
  • the multi-stage countercurrent ultrafiltration is carried out on the sugar-containing solution, and the multi-stage countercurrent ultrafiltration is carried out through a 2-5-stage ultrafiltration membrane module having a molecular weight cut-off of 1000-5000 Da and an operating temperature of 25- 95 ° C, operating pressure 0.5-1.5 MPa, the first stage ultrafiltration permeate and the last stage ultrafiltration retentate, the last stage of ultrafiltration retentate discharge;
  • the first stage ultrafiltration permeate is subjected to nanofiltration concentration, and the nanofiltration concentration is carried out through a nanofiltration membrane module having a molecular weight cutoff of 90-400 Da and an operating temperature of 25-95 ° C. Operating pressure 2.0-4.1 MPa, obtaining a sugar-containing concentrate and a nanofiltration permeate;
  • the residual sugar recovery device in the sugar cane sugar production process provided by the invention is simple, safe and easy to operate. There is no chemical additive in the produced and recycled sugar.
  • the method for recovering residual sugar in the process of sugar cane sugar production provided by the invention not only reduces the residual sugar loss in the ultrafiltration process of the sucrose mixed juice, but also saves more than 50% of the washing and filtering water consumption, and ensures the loss of sucrose in the decolorization section.
  • the rate is less than 2%, and a high glucose concentration of the diafiltration permeate is obtained.
  • the last-stage ultrafiltration membrane module retentate obtained by the residual sugar recovery device in the sugar cane sugar-making process provided by the invention has extremely low sugar content and no chemical, and can be used for extracting natural pigments.
  • FIG. 1 is a schematic view showing the structure of a device for recovering residual sugar in the process of sugar cane production provided in Example 1.
  • FIG. 1 A device for recovering residual sugar in sugar cane sugar making process is shown in FIG. 1 .
  • the device comprises a multi-stage countercurrent washing unit and a nanofiltration concentration unit, the multi-stage counter-current washing unit comprises a 3-stage ultrafiltration membrane module, and the 3-stage ultrafiltration membrane module is a first stage connected in series through a pipeline. a second stage and a third stage ultrafiltration membrane module; the nanofiltration concentration unit is a nanofiltration membrane module;
  • the ultrafiltration membrane module is a 4040 food grade coiled polyethersulfone membrane module, the first-stage ultrafiltration membrane module is formed by connecting six membrane modules in parallel, and the second-stage ultrafiltration membrane module is formed by paralleling four membrane modules.
  • the three-stage ultrafiltration membrane module is formed by two membrane modules in parallel; the nanofiltration membrane module is a food grade 4040-type coiled organic membrane module, which is formed by connecting two membrane modules in parallel.
  • the intercepting side outlet of the first stage ultrafiltration membrane module is connected to the intercepting side inlet of the second stage ultrafiltration membrane module through a line, the intercepting side outlet of the second stage ultrafiltration membrane module and the intercepting side of the third stage ultrafiltration membrane module
  • the inlet is connected;
  • the permeate side outlet of the third stage ultrafiltration membrane module is connected to the interception side inlet of the second stage ultrafiltration membrane module,
  • the permeate side outlet of the second stage ultrafiltration membrane module is connected to the interception side inlet of the first stage ultrafiltration membrane module;
  • the permeate side outlet of the first stage ultrafiltration membrane module is in communication with the intercepting side inlet of the nanofiltration membrane module through a line, and the permeate side outlet of the nanofiltration membrane module passes through the line and the intercepting side of the third stage ultrafiltration membrane module Imports are connected;
  • the cut-off side of the nanofiltration membrane module obtains a sugar-containing concentrated liquid, which is crystallized by evaporation to obtain a sugar; the retentate obtained by the third-stage ultrafiltration membrane module is discharged for extracting a natural pigment.
  • a device for recovering residual sugar in a sugar cane sugar-making process comprising a multi-stage countercurrent washing unit and a nanofiltration concentration unit, the multi-stage countercurrent washing unit comprising a 2-stage ultrafiltration membrane module, the level 2 super
  • the membrane module is a first-stage and second-stage ultrafiltration membrane module connected in series through a pipeline;
  • the nanofiltration concentration unit is a nanofiltration membrane module;
  • the ultrafiltration membrane module is a hollow fiber type polyvinylidene chloride membrane module, and the first stage and second stage ultrafiltration membrane modules are each formed by four membrane modules in parallel;
  • the nanofiltration membrane module is a food grade 4040 type a roll type organic film module formed by connecting two film modules in parallel;
  • the intercepting side outlet of the first stage ultrafiltration membrane module is connected to the intercepting side inlet of the second stage ultrafiltration membrane module through a line, the intercepting side outlet of the second stage ultrafiltration membrane module and the intercepting side of the first stage ultrafiltration membrane module Imported;
  • the permeate side outlet of the first stage ultrafiltration membrane module is in communication with the intercepting side inlet of the nanofiltration membrane module through a line, and the permeate side outlet of the nanofiltration membrane module passes through the line and the intercepting side of the second stage ultrafiltration membrane module Imports are connected;
  • the cut-off side of the nanofiltration membrane module obtains a sugar-containing concentrated liquid, which is crystallized by evaporation to obtain a sugar; the retentate obtained by the second-stage ultrafiltration membrane module is discharged for extracting a natural pigment.
  • a device for recovering residual sugar in a sugar cane sugar-making process comprising a multi-stage countercurrent washing unit and a nanofiltration concentration unit, the multi-stage countercurrent washing unit comprising a 5-stage ultrafiltration membrane module, the 5-stage super
  • the membrane module is a first stage, a second stage, a third stage, a fourth stage and a fifth stage ultrafiltration membrane module connected in series through a pipeline;
  • the nanofiltration concentration unit is a nanofiltration membrane module;
  • the ultrafiltration membrane module is a flat sulfonated polyethersulfone membrane module, and the first to fifth ultrafiltration membrane modules are each formed by three membrane modules in parallel;
  • the nanofiltration membrane module is a food grade 4040 type a roll type organic film module formed by connecting four film modules in parallel;
  • the intercepting side outlet of the first stage ultrafiltration membrane module is connected to the intercepting side inlet of the second stage ultrafiltration membrane module through a line, the intercepting side outlet of the second stage ultrafiltration membrane module and the intercepting side of the third stage ultrafiltration membrane module
  • the inlet side is connected, and the cut-off side outlet of the third-stage ultrafiltration membrane module is connected to the cut-off side inlet of the fourth-stage ultrafiltration membrane module, and the cut-off side outlet of the fourth-stage ultrafiltration membrane module and the intercepting side of the fifth-stage ultrafiltration membrane module
  • the inlet side is connected; the permeate side outlet of the fifth stage ultrafiltration membrane module is connected to the interception side inlet of the fourth stage ultrafiltration membrane module, the permeate side outlet of the fourth stage ultrafiltration membrane module and the third stage ultrafiltration membrane module
  • the intercepting side inlet is connected, the permeate side outlet of the third stage ultrafiltration membrane module is connected to the intercepting side inlet of the second stage ultrafiltration membrane module, the permeate side outlet of the second stage ultrafiltration
  • the permeate side outlet of the first stage ultrafiltration membrane module is in communication with the intercepting side inlet of the nanofiltration membrane module through a line, and the permeate side outlet of the nanofiltration membrane module passes through the line and the intercepting side of the fifth stage ultrafiltration membrane module Imports are connected;
  • the cut-off side of the nanofiltration membrane module obtains a sugar-containing concentrate, which is crystallized by evaporation to obtain a sugar; the retentate obtained by the fifth-stage ultrafiltration membrane module is discharged for extracting a natural pigment.
  • the recovery of the residual sugar by the recovery device described in Example 1 includes the following steps:
  • the three-stage countercurrent washing unit is filled with deionized water to start the washing system, and the third-stage countercurrent washing
  • the ultrafiltration membrane module of the unit has a molecular weight cutoff of 2000 Da, an operating temperature of 60 ° C, an operating pressure of 1.0 MPa, and then a 20-fold concentrated sugar cane juice concentrate (sucrose fraction 15%, sugar cane) by microfiltration pretreatment and ultrafiltration decolorization
  • the mixed juice liquid sucrose is divided into 10%) and pumped into the three-stage countercurrent washing unit at a flow rate of 0.25 t/h, while adding 0.25 t/h of deionized water to the third-stage ultrafiltration membrane module, the first stage
  • the washed filter permeate obtained by the ultrafiltration membrane module was pumped into the nanofiltration membrane module at a flow rate of 0.5 t/h.
  • the molecular weight cutoff of the nanofiltration membrane module was 250 Da, the operating temperature was 60 ° C, the operating pressure was 3.0 MPa, and the concentration multiple was 2. Producing 0.25t/h nanofiltration permeate as the washing water for part of the third-stage ultrafiltration membrane module.
  • the total flow rate of the third-stage ultrafiltration membrane module is 0.5t/h, and 0.5t is generated at the same time. /h of the third stage washing filter permeate as the second stage ultrafiltration membrane module washing water, 0.5t / h of the second stage washing filter permeate as the first stage washing water.
  • the sugar content in the third-stage washing residue is about 2.32%
  • the nanofiltration concentrate contains about 12.6% sucrose
  • the color value is 798IU
  • the recovery rate of residual sugar is 84.5%.
  • the filter membrane module is a roll-type polyethersulfone membrane module, the molecular weight cut-off is 2000 Da, the operating temperature is 60 ° C, the pressure is 1.0 MPa, the dilution ratio is 2), and the same residual sugar recovery rate is obtained.
  • the water consumption is about 4 times that of the new process, the decolorization rate is reduced to 92%, and the sugar content in the ultrafiltration washing liquid is only 3.17%.
  • the recovery of the residual sugar by the recovery device described in Example 1 includes the following steps:
  • the three-stage countercurrent washing unit is filled with deionized water to start the system.
  • the ultrafiltration membrane module of the three-stage countercurrent washing unit has a molecular weight cutoff of 1500 Da, an operating temperature of 65 ° C, an operating pressure of 0.8 MPa, and then microfiltration.
  • Pretreatment and ultrafiltration decolorization and concentration 20 times of sugarcane juice concentrate (16% sucrose, 11% sucrose in sugarcane juice) is pumped into the three-stage countercurrent washing unit at a flow rate of 0.25t/h.
  • 0.5t/h of deionized water was added to the tertiary ultrafiltration membrane module, and the washed filtrate permeate obtained by the first stage of washing was pumped into the nanofiltration membrane module at a flow rate of 0.75 t/h, and the nanofiltration membrane module was
  • the molecular weight cut-off is 200Da
  • the concentration of the nanofiltration concentration is 55 ° C
  • the operating pressure is 3.2 MPa
  • the concentration multiple is 1.5.
  • the nanofiltration permeate of 0.25 t/h is produced as the washing water for the partial third-stage ultrafiltration membrane module.
  • the total flow rate of the third stage washing water is 0.75t/h, and the third stage washing liquid permeate of 0.75t/h is produced as the second stage washing water, and the second stage washing liquid permeating liquid of 0.75t/h. As the first stage of washing water.
  • the sugar content in the third-stage washing residue is about 1.12%
  • the sucrose content in the nanofiltration concentrate is about 7.41%
  • the color value is 848 IU
  • the residual sugar recovery rate is 92.6%
  • the residual sugar loss accounts for the whole.
  • the process has a total sugar content of 0.5%
  • the recovered nanofiltration concentrate has a decolorization rate of 94%.
  • washing membrane module is a roll-type polyethersulfone membrane module, molecular weight cut-off 1500 Da, operating temperature 65 ° C, pressure 0.8 MPa, dilution factor 2)
  • the water consumption is about 3 times that of the new process, the decolorization rate is reduced to 88%, and the sugar content in the washing and decolorizing liquid is only 2.48%.
  • Example 1 The recovery apparatus described in Example 1 saved 66.7% of water, the decolorization rate increased by 6.8%, and the sugar concentration in the recovered washed filtrate increased by 199%.
  • the recovery of the residual sugar by the recovery device described in Example 1 includes the following steps:
  • the three-stage countercurrent washing unit is filled with deionized water to start the system.
  • the ultrafiltration membrane module of the three-stage countercurrent washing unit has a molecular weight cutoff of 1000 Da, an operating temperature of 95 ° C, an operating pressure of 1.5 MPa, and then microfiltration.
  • Pretreatment and ultrafiltration decolorization and concentration 30 times of sugarcane juice concentrate (16% sucrose, 10% sucrose in sugarcane juice) is pumped into a three-stage countercurrent washing unit at a flow rate of 0.25t/h.
  • 0.4t/h of deionized water was added to the tertiary ultrafiltration membrane module, and the washed filtrate permeate obtained by the first stage of washing was pumped into the nanofiltration membrane module at a flow rate of 0.5 t/h, and the nanofiltration membrane module was
  • the molecular weight cut-off is 90Da
  • the concentration of the nanofiltration is 95 ° C
  • the operating pressure is 4.1 MPa
  • the concentration is 1.25.
  • the nanofiltration permeate of 0.1 t/h is used as the washing water for the third-stage ultrafiltration membrane module.
  • the total flow rate of the third stage washing water is 0.5t/h, and the third stage washing liquid permeate of 0.5t/h is produced as the second stage washing water, and the second stage washing liquid permeating liquid of 0.5t/h. As the first stage of washing water.
  • the sugar content of the third-stage washing residue is about 2.82%
  • the nanofiltration concentrate contains sucrose of about 8.2%
  • the color value is 736 IU
  • the residual sugar recovery rate is 82%
  • the residual sugar loss accounts for the whole. 0.9% of the total sugar of the process
  • the decolorization rate of the recovered nanofiltration concentrate was 94.8%.
  • the filter membrane module is a roll-type polyethersulfone membrane module, the molecular weight cut-off is 1000 Da, the operating temperature is 95 ° C, the pressure is 1.5 MPa, the dilution ratio is 2), and the same residual sugar recovery rate is obtained.
  • the water consumption is about 3 times that of the new process, the decolorization rate is reduced to 89%, and the washing and decolorizing liquid contains only sugar. It is 2.75%.
  • Example 1 The recovery apparatus described in Example 1 saved 66.7% of water, the decolorization rate increased by 6.5%, and the sugar concentration in the recovered washed filtrate increased by 198%.
  • the recovery of the residual sugar by the recovery device described in Example 1 includes the following steps:
  • the three-stage countercurrent washing unit is filled with deionized water to start the system.
  • the ultrafiltration membrane module of the three-stage countercurrent washing unit has a molecular weight cutoff of 5000 Da, an operating temperature of 25 ° C, an operating pressure of 0.5 MPa, and then microfiltration.
  • Pretreatment and ultrafiltration decolorization and concentration 10 times of sugarcane juice concentrate (14% sucrose, 11% sucrose in sugarcane juice) is pumped into the three-stage countercurrent washing unit at a flow rate of 0.25t/h.
  • 0.25t/h of deionized water was added to the tertiary ultrafiltration membrane module, and the washed filtrate permeate obtained by the first stage of washing was pumped into the nanofiltration membrane module at a flow rate of 0.5 t/h, and the nanofiltration membrane module was
  • the molecular weight cut-off is 400Da
  • the concentration of the nanofiltration is 25 ° C
  • the operating pressure is 2.0 MPa
  • the concentration is 2, which produces 0.25 t / h of nanofiltration permeate as part of the third-stage ultrafiltration membrane module.
  • the total flow rate of the third stage washing water is 0.5t/h, and the third stage washing liquid permeate of 0.5t/h is produced as the second stage washing water, and the second stage washing liquid permeating liquid of 0.5t/h. As the first stage of washing water.
  • the sugar content in the third-stage washing residue is about 2.19%
  • the sucrose content in the nanofiltration concentrate is about 11.32%
  • the color value is 932 IU
  • the residual sugar recovery rate is 80.9%
  • the residual sugar loss accounts for the whole.
  • the process total sugar was 1.91%
  • the recovered nanofiltration concentrate had a decolorization rate of 93.4%.
  • washing membrane module is a roll-type polyethersulfone membrane module, molecular weight cut-off of 5000 Da, operating temperature 25 ° C, pressure 0.5 MPa, dilution factor of 2)
  • the water consumption is about 3.5 times that of the new process, the decolorization rate is reduced to 79.2%, and the sugar content in the washing and decolorizing liquid is only 3.2%.
  • Example 1 saves water by 71.4%, and the decolorization rate increases by 17.9%.
  • the sugar concentration in the wash filtrate increased by 254%.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Biochemistry (AREA)
  • Organic Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

La présente invention concerne un appareil et un procédé pour la récupération de sucre résiduel dans un processus de production de sucre de canne. L'appareil comprend une unité de filtration-lavage à contre-courant à étages multiples et une unité de nanofiltration-concentration, ladite unité de filtration-lavage à contre-courant à étages multiples comprenant des composants à membrane d'ultrafiltration dans au moins deux étages, et ladite unité de nanofiltration-concentration comprenant un composant à membrane de nanofiltration ; une sortie du côté rétentat du composant à membrane d'ultrafiltration de l'étage précédent de l'unité de filtration-lavage à contre-courant à étages multiples étant reliée à une entrée du côté rétentat du composant à membrane d'ultrafiltration de l'étage suivant, une entrée du côté rétentat du composant à membrane d'ultrafiltration de l'étage précédent étant reliée à une sortie du côté perméat du composant à membrane d'ultrafiltration de l'étage suivant ; et une sortie du côté perméat du composant à membrane d'ultrafiltration du premier étage de l'unité de filtration-lavage à contre-courant à étages multiples étant reliée à une entrée du côté rétentat du composant à membrane de nanofiltration. Ledit appareil permet d'obtenir un taux de pertes du sucre de canne inférieur à 2 % dans une section de décoloration, permet d'économiser au moins 50 % de la consommation d'eau de filtration-lavage, et d'obtenir un perméat de filtration-lavage de concentration élevée en sucre. L'opération est facile à mettre en œuvre et sûre, la production peut être continue, et le concentré contenant du sucre obtenu est exempt d'additifs chimiques.
PCT/CN2016/103398 2015-10-28 2016-10-26 Appareil et procédé pour la récupération de sucre résiduel dans un processus de production de sucre de canne WO2017071585A1 (fr)

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CN105603130B (zh) * 2015-10-28 2019-07-19 中国科学院过程工程研究所 一种甘蔗制糖过程中残糖的回收装置及方法
CN106515081B (zh) * 2016-12-28 2018-03-20 钦州华成自控设备有限公司 一种甘蔗压榨机渗透水的在线自动控制系统及控制方法
CN108031289A (zh) * 2017-12-06 2018-05-15 四川美富特水务有限责任公司 蔗糖液膜浓缩系统及该膜浓缩系统的清洗方法
AU2021432103A1 (en) * 2021-03-08 2023-08-24 Boehringer Ingelheim International Gmbh Systems and methods for single pass counter current diafiltration
CN116651164B (zh) * 2023-07-18 2024-02-20 临沂市凯特莱机械制造有限责任公司 一种果蔬冻干挑选车间漂浮粉尘的回收装置

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