CN218910202U - System for coproducing xylose crystals and caramel pigment by utilizing xylose massecuite - Google Patents
System for coproducing xylose crystals and caramel pigment by utilizing xylose massecuite Download PDFInfo
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- CN218910202U CN218910202U CN202223322843.2U CN202223322843U CN218910202U CN 218910202 U CN218910202 U CN 218910202U CN 202223322843 U CN202223322843 U CN 202223322843U CN 218910202 U CN218910202 U CN 218910202U
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Abstract
The utility model relates to a system for co-producing xylose crystals and caramel pigment by utilizing xylose massecuite, which comprises a raw material storage tank, a coagulation tank, a flocculation tank, a neutralization tank, a first filter, a nanofiltration membrane separator, an electrodialysis membrane separator, a chromatographic separation device, an evaporation concentration tank, a crystallization tank, a centrifugal separator, a dryer, a sugar liquid mixing tank, a browning reaction kettle, a second filter and a wiped film evaporator, wherein the raw material storage tank is connected with the coagulation tank; the extraction liquid outlet of the chromatographic separation device is communicated with the evaporation concentration tank, the raffinate outlet is communicated with the sugar liquid mixing tank, the solid outlet of the centrifugal separator is communicated with the dryer, the liquid outlet is communicated with the sugar liquid mixing tank, the raw material storage tank stores xylose massecuite raw material to be processed, the material output by the dryer is xylose crystals, and the material obtained by the wiped film evaporator is high-red caramel pigment. The utility model fully utilizes the xylose massecuite which cannot be utilized and affects the environmental ecology, and also produces xylose crystals with high added value and high red finger caramel pigment.
Description
Technical Field
The utility model belongs to the technical field of sugar alcohol preparation, and particularly relates to a system for co-producing xylose crystals and caramel pigment by utilizing xylose massecuite.
Background
Xylose is mainly obtained by hydrolyzing plants such as corncob, straw, rice husk and the like, concentrating into massecuite and refining. Certain foreign enterprises use bagasse as a raw material for papermaking, and byproduct xylose massecuite is more than 30000 tons/year, fine silicide is mixed in the massecuite due to the problem of raw materials, and the silicide is difficult to remove, so that the filtering equipment is blocked, the overall production efficiency is influenced, and finally the xylose massecuite cannot be effectively utilized. In addition, the xylose massecuite is rich in 80 weight percent of sugar resources, wherein pentose accounts for 45 weight percent and hexose accounts for about 30 weight percent. The xylose massecuite is used as the raw material, after impurities affecting the use are removed, pentose in the xylose massecuite raw material is prepared into xylose crystals, hexose and residual pentose to prepare Cheng Gaogong caramel pigment, so that the xylose massecuite which cannot be utilized and affects the environmental ecology can be fully utilized, and xylose crystals with high added value and high red caramel pigment can be produced.
Disclosure of Invention
The technical problem to be solved by the utility model is to provide a system for co-producing xylose crystals and caramel pigment by utilizing xylose massecuite, wherein after removing impurity silicide in the xylose massecuite by adopting a coagulation-flocculation process, pentose in the xylose massecuite is prepared into xylose crystals, hexose and residual pentose to prepare Cheng Gaogong which refers to caramel pigment. The utility model not only fully utilizes the xylose massecuite which cannot be utilized and affects the environmental ecology, but also produces xylose crystals with high added value and high red finger caramel pigment, thereby effectively utilizing the xylose massecuite which is a byproduct of the paper industry.
The utility model is realized in this way, the utility model provides a system for co-producing xylose crystals and caramel pigment by utilizing xylose massecuite, which comprises a xylose preparation subsystem and a caramel pigment preparation subsystem which are connected with each other through pipelines, wherein the xylose preparation subsystem comprises a raw material storage tank, a coagulation tank, a flocculation tank, a neutralization tank, a first filter, a nanofiltration membrane separator, an electrodialysis membrane separator, a chromatographic separation device, an evaporation concentration tank, a crystallization tank, a centrifugal separator and a dryer which are connected with each other through pipelines in sequence, and the caramel pigment preparation subsystem comprises a sugar liquid mixing tank, a browning reaction kettle, a second filter and a wiped film evaporator which are connected with each other through pipelines in sequence; the chromatographic separation device is provided with an extracting solution outlet and a raffinate outlet respectively, the extracting solution outlet is communicated with a feed inlet of the evaporation concentration tank through a pipeline, the raffinate outlet is communicated with a feed inlet of the sugar liquid mixing tank through a pipeline, the centrifugal separator is provided with a solid outlet and a liquid outlet respectively, the solid outlet is communicated with a feed inlet of the dryer through a pipeline, the liquid outlet is communicated with one feed inlet of the sugar liquid mixing tank, the raw material storage tank stores xylose massecuite raw material to be processed, the material output by a discharge outlet of the dryer is xylose crystals, and the material finally obtained by a discharge outlet of the scraping film evaporator is high red caramel pigment.
Further, the extract liquid output from the extract liquid outlet of the chromatographic separation device is chromatographic extract liquid, and the raffinate liquid output from the raffinate liquid outlet of the chromatographic separation device is chromatographic raffinate liquid.
Further, the liquid delivered from the liquid outlet of the centrifugal separator is xylose centrifugation mother liquor.
Compared with the prior art, the system for co-producing xylose crystals and caramel pigment by utilizing xylose massecuite has the following characteristics:
1. the silicide impurities influencing the filtration are removed through the coagulation-flocculation process, and the filtration rate of the xylose massecuite is improved by approximately 3 times, so that the preparation of the xylose massecuite into xylose crystals is possible to industrialize.
2. The pentose in the xylose massecuite is prepared into xylose crystals, hexose and residual pentose to prepare Cheng Gaogong caramel pigment, so that the resource utilization rate is improved, meanwhile, a high-red caramel pigment product with the red index of up to 7 is also prepared, and the comprehensive utilization value of saccharide resources of the xylose massecuite is greatly improved.
3. Through improvement and optimization of the whole process system, pentose in the xylose massecuite is prepared into xylose crystals, hexose and residual pentose to prepare Cheng Gaogong caramel pigment, and the xylose crystals with the selling price of 200-500 yuan/ton are converted into 20000-25000 yuan/ton and 4000-5000 yuan/ton of high red caramel pigment, so that the economic benefit is greatly improved.
Drawings
FIG. 1 is a schematic diagram of a preferred embodiment of a system for co-producing xylose crystals and caramel color using xylose massecuite in accordance with the present utility model;
FIG. 2 is a schematic view of the flow direction of each material in a system for co-producing xylose crystals and caramel color using xylose massecuite according to the present utility model.
Detailed Description
In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the utility model is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the utility model.
Referring to fig. 1 and 2, a preferred embodiment of the system for co-producing xylose crystals and caramel color using xylose massecuites according to the present utility model comprises a xylose preparation subsystem i and a caramel color preparation subsystem ii connected to each other via a pipeline. The arrow direction in the figure is a schematic representation of the flow direction of the material in the system.
The xylose preparation subsystem I comprises a raw material storage tank 1, a coagulation tank 2, a flocculation tank 3, a neutralization tank 4, a first filter 5, a nanofiltration membrane separator 6, an electrodialysis membrane separator 7, a chromatographic separation device 8, an evaporation concentration tank 9, a crystallization tank 10, a centrifugal separator 11 and a dryer 12 which are sequentially connected through pipelines, and the caramel pigment preparation subsystem II comprises a sugar liquid mixing tank 13, a browning reaction kettle 14, a second filter 15 and a wiped film evaporator 16 which are sequentially connected through pipelines.
The chromatographic separation device 8 is respectively provided with an extracting solution outlet and a raffinate outlet, the extracting solution outlet is communicated with the feed inlet of the evaporation concentration tank 9 through a pipeline, and the raffinate outlet is communicated with the feed inlet of the sugar liquid mixing tank 13 through a pipeline. The centrifugal separator 11 is provided with a solid outlet and a liquid outlet, the solid outlet is communicated with a feed inlet of the dryer 12 through a pipeline, and the liquid outlet is communicated with a feed inlet of the sugar liquid mixing tank 13. The other feed inlet of the sugar liquid mixing tank 13 is communicated with the raffinate outlet of the chromatographic separation device 8 through a pipeline. The raw material storage tank 1 stores the raw material of xylose massecuite A to be processed, the material output by the discharge port of the dryer 12 is xylose crystal B, and the material finally obtained by the discharge port of the wiped film evaporator 16 is high red caramel pigment C.
The chromatographic extract D is outputted from the extract outlet of the chromatographic separation device 8, and the chromatographic raffinate E is outputted from the raffinate outlet of the chromatographic separation device 8.
The liquid fed from the liquid outlet of the centrifugal separator 11 is xylose mother liquor F.
The coagulation tank 2 is used for gathering fine silicide together, the flocculation tank 3 is used for precipitating the gathered fine silicide together, the neutralization tank 4 is used for neutralizing the pH of the xylose massecuite liquid, and the first filter 5 is used for filtering the flocculate. The nanofiltration membrane separator 6 is used for decoloring xylose liquid, the trapped liquid is pigment liquid, and the permeate liquid is decoloring liquid. The electrodialysis membrane separator 7 is used for desalting xylose liquid, the trapped liquid is concentrated salt liquid, and the permeate liquid is desalted liquid. The chromatographic separation device 8 is used for separating the chromatographic separation extracting solution with high xylose content and the chromatographic separation raffinate with low xylose content from the chromatographic separation feed solution G flowing through. The evaporation concentration tank 9 and the crystallization tank 10 are used for evaporation concentration and xylose crystallization, and the centrifugal separator 11 is used for separating crystalline xylose and xylose centrifugal mother liquor. The dryer 12 is used to dry the crystalline xylose to obtain a xylose crystal B product.
The sugar solution mixing tank 13 is used for mixing chromatographic separation raffinate and xylose centrifugal mother solution, and the browning reaction kettle 14 is used for preparing a high-red caramel pigment crude product through browning reaction of the mixed sugar solution. The second filter 15 is used to remove solid impurities from the caramel color and the wiped film evaporator 16 is used to reduce the caramel color by Wen Dinong to provide a high reddish caramel color C.
The present utility model is thus achieved providing a method for co-producing xylose crystals and caramel color using xylose massecuite, said method using a system for co-producing xylose crystals and caramel color using xylose massecuite as described above, said method comprising the steps of:
step one, xylose massecuite A in a raw material storage tank 1 is conveyed to a coagulation tank 2 through a pipeline to be subjected to silicide aggregation treatment, and then is sequentially conveyed to a flocculation tank 3 and a neutralization tank 4 through a pipeline to be respectively subjected to flocculation treatment and neutralization treatment.
And step two, conveying the neutralized feed liquid to a first filter 5 through a pipeline for filtering treatment, and sequentially conveying the filtered feed liquid to a nanofiltration membrane separator 6 and an electrodialysis membrane separator 7 through pipelines for decoloring treatment and desalting treatment respectively.
Step three, sending the desalted chromatographic separation feed solution G into a chromatographic separation device 8 for chromatographic separation treatment, and sequentially sending a chromatographic separation extracting solution D with high xylose content obtained after the chromatographic separation treatment into an evaporation concentration tank 9 for evaporation concentration treatment, a crystallization tank 10 for crystallization treatment and a centrifugal separator 11 for centrifugal separation treatment through a pipeline; and conveying the chromatographic raffinate E with low xylose content obtained after chromatographic separation treatment into a sugar liquid mixing tank 13 through a pipeline, and mixing with xylose centrifugal mother liquor F to prepare the high-red-finger caramel pigment.
And step four, delivering the xylose solid subjected to centrifugal separation to a dryer 12 for drying treatment to obtain a xylose crystal B finished product.
And fifthly, conveying the mixed sugar solution of the chromatographic separation raffinate and the xylose centrifugal mother solution in the sugar solution mixing tank 13 into a browning reaction kettle 14 through a pipeline for browning reaction, and sequentially carrying out filtration treatment of a second filter 15 and evaporation treatment of a wiped film evaporator 16 through the pipeline to obtain the high-red-finger caramel pigment.
In the first step, the dry matter mass percentage concentration of the sugar resources in the xylose massecuite A is 80-90 wt%. Wherein, in the dry matter of the saccharide resource, the hexose contains 30-35 wt% and the pentose contains 45-50 wt%. During the coagulation treatment, adding 1.0 g/L-10.0 g/L of iron-magnesium compound agent as coagulant into xylose massecuite liquid, wherein the iron-magnesium compound agent adopts magnesium chloride and ferrous sulfate to compound, and the compounding ratio is m Magnesium chloride ：m Ferrous sulfate 1:1-9:1, fully stirring to be uniform, and adjusting the pH value of the xylose massecuite liquid to 9-10 by using sodium hydroxide; during flocculation treatment, adding 1.0-10.0 g/L diatomite for adsorption, slowly stirring for 30min, settling and separating, conveying the supernatant to a neutralization tank 4, and adding hydrochloric acid to adjust the pH to be neutral.
In the second step, during nanofiltration decolorization treatment, the operating temperature of the nanofiltration membrane separator 6 is 40-60 ℃ and the operating pressure is 15-35 bar; in the electrodialysis desalination treatment, the operation current of the electrodialysis membrane separator 7 is 60-120A, the voltage is 200-250V, and the operation pressure is 15-35 bar.
In the fifth step, during browning reaction treatment, the used reaction auxiliary agent is the mixture of food-grade succinic acid and citric acid, the mixture ratio is 7:3-5:5, and the reaction process is regulated as follows: firstly, regulating the pH value to 2.0-4.0, then heating to 80-90 ℃ for reaction for 30-50 min, then heating to 150-170 ℃ for reaction for 2-4 h, continuously dripping a food-grade defoaming agent, and adding water until the refraction is about 40% after the reaction is finished; in the wiped film evaporation treatment, the evaporation pressure of the wiped film evaporator 16 is 4-5 bar, and the vacuum degree is 80-90 kpa.
The system for co-producing xylose crystals and caramel color using xylose massecuite of the present utility model is further described below by way of specific examples.
The first method for co-producing xylose crystals and caramel pigment by utilizing xylose massecuite adopts the xylose massecuite as a raw material, and then the high-red-finger caramel pigment is prepared by mixing a chromatographic separation raffinate and a xylose centrifugal mother solution after preparing finished xylose crystals. The method comprises the following steps:
step one, conveying xylose massecuite A in a raw material storage tank 1 to a coagulation tank 2 through a pipeline for silicide aggregation treatment, adding 10.0g/L of iron-magnesium compound agent as a coagulant into xylose massecuite liquid during coagulation treatment, wherein the iron-magnesium compound agent is compounded by adopting magnesium chloride and ferrous sulfate, and the compounding ratio m Magnesium chloride ：m Ferrous sulfate 1:1, stirring thoroughly to make it uniform, adjusting the pH of sugar solution to 9 with sodium hydroxide, and then sending into a flocculation tank for flocculation treatment. During flocculation treatment, 10.0g/L diatomite is added for adsorption, the mixture is slowly stirred for 30min and then separated by sedimentation, and the supernatant is conveyed to a neutralization tank 4 and added with hydrochloric acid to adjust the pH to 7.
Step two, the material liquid after neutralization treatment is conveyed to a first filter 5 through a pipeline for filtration treatment, and is sequentially conveyed to a nanofiltration membrane separator 6 and an electrodialysis membrane separator 7 through a pipeline for decolorization treatment and desalination treatment after filtration, wherein the filtration rate of the material liquid after neutralization treatment passing through a 0.8 mu m filter membrane is 1.13m 3 /（m 2 * h) Meets the requirement of daily production efficiency. During nanofiltration decolorization treatment, the operating temperature of the nanofiltration membrane separator is 60 ℃ and the operating pressure is 15bar; in the electrodialysis desalination treatment, the electrodialysis membrane separator operates at a current of 120A, a voltage of 200V and an operating pressure of 15bar.
Step three, sending the desalted chromatographic separation feed solution G into a chromatographic separation device 8 for chromatographic separation, and sequentially sending a chromatographic separation extracting solution D with the xylose percentage of 85wt% obtained after the chromatographic separation to an evaporation concentration tank 9 for evaporation concentration, a crystallization tank 10 for crystallization and a centrifugal separator 11 for centrifugal separation through a pipeline. And conveying the chromatographic separation raffinate E with the xylose percentage of 10wt% obtained after chromatographic separation treatment into a sugar liquid mixing tank 13 through a pipeline, and mixing with the xylose centrifugal mother liquor F (with the xylose percentage of 40 wt%) to prepare the high-red-finger caramel pigment.
And step four, delivering the centrifugally separated xylose solid to a dryer 12 for drying treatment to obtain a xylose crystal B finished product. The purity of xylose of the prepared xylose crystal finished product reaches 98 percent.
Step six, the mixed sugar solution of the chromatographic separation raffinate and the xylose centrifugal mother solution in the sugar solution mixing tank 13 is conveyed into a browning reaction kettle 14 together through a pipeline to carry out browning reaction, and during the browning reaction treatment, the used reaction auxiliary agent is the compound of food-grade succinic acid and citric acid, the compound ratio is 7:3, and the reaction process is regulated and controlled as follows: the pH is regulated to 2.0, then the temperature is raised to 90 ℃ for reaction for 30min, then the temperature is raised to 170 ℃ for reaction for 2h, the food-grade defoamer is continuously added dropwise, and then water is added until the refraction is about 40% after the reaction is finished. And then the high red-finger caramel pigment is prepared after the filtering treatment of the second filter 15 and the evaporation treatment of the wiped film evaporator 16 are sequentially carried out through a pipeline. In the wiped film evaporation treatment, the evaporation pressure of the wiped film evaporator 16 was 4bar and the vacuum degree was 90kpa. Finally, the red index of the high red caramel pigment product is up to 7.5, other indexes are combined with the national standard, and the utilization rate of sugar resources is up to 95%.
Comparative example 1:
xylose is directly extracted by adopting xylose massecuite A as a raw material, and the specific steps comprise: after the xylose massecuite A in the raw material storage tank 1 is used as a raw material and is conveyed to the first filter through a pipeline, the filtering rate of the xylose massecuite A passing through a 0.8 mu m filter membrane is 0.39m 3 /（m 2 * h) A. The utility model relates to a method for producing a fibre-reinforced plastic composite Then the xylose crystal finished product is finally obtained after nanofiltration decolorization, electrodialysis desalination treatment, chromatographic separation, evaporation concentration, crystallization and centrifugation treatment. Because the filtration is low, the system is difficult to operate effectively, the production efficiency is reduced by about 60 percent, the raffinate after chromatographic separation is sold for syrup, the xylose centrifugal mother liquor is recycled, and the actual utilization rate of sugar resources is only 70 percent.
In conclusion, through the improvement of the whole system and the whole method, the production efficiency is improved from 40% to 100%, the utilization rate of sugar resources in the xylose massecuite A is improved from 70% to 95%, and the red index of the caramel pigment is as high as 7.0. The utility model not only improves the possibility of preparing xylose by using the xylose massecuite A as a raw material, but also improves the comprehensive utilization value of saccharide resources of the xylose massecuite A.
The foregoing description of the preferred embodiments of the utility model is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the utility model.
Claims (3)
1. The system for co-producing xylose crystals and caramel pigment by utilizing xylose massecuite is characterized by comprising a xylose preparation subsystem and a caramel pigment preparation subsystem which are connected with each other through a pipeline, wherein the xylose preparation subsystem comprises a raw material storage tank, a coagulation tank, a flocculation tank, a neutralization tank, a first filter, a nanofiltration membrane separator, an electrodialysis membrane separator, a chromatographic separation device, an evaporation concentration tank, a crystallization tank, a centrifugal separator and a dryer which are connected with each other through pipelines in sequence, and the caramel pigment preparation subsystem comprises a sugar liquid mixing tank, a browning reaction kettle, a second filter and a film scraping evaporator which are connected with each other through pipelines in sequence; the chromatographic separation device is provided with an extracting solution outlet and a raffinate outlet respectively, the extracting solution outlet is communicated with a feed inlet of the evaporation concentration tank through a pipeline, the raffinate outlet is communicated with a feed inlet of the sugar liquid mixing tank through a pipeline, the centrifugal separator is provided with a solid outlet and a liquid outlet respectively, the solid outlet is communicated with a feed inlet of the dryer through a pipeline, the liquid outlet is communicated with one feed inlet of the sugar liquid mixing tank, the raw material storage tank stores xylose massecuite raw material to be processed, the material output by a discharge outlet of the dryer is xylose crystals, and the material finally obtained by a discharge outlet of the scraping film evaporator is high red caramel pigment.
2. The system for co-producing xylose crystals and caramel color using xylose massecuite as claimed in claim 1, wherein the extract outlet from the chromatographic separation device is chromatographic extract, and the raffinate outlet from the chromatographic separation device is chromatographic raffinate.
3. The system for co-producing xylose crystals and caramel color using xylose massecuite as claimed in claim 1, wherein the liquid delivered from the liquid outlet of the centrifugal separator is xylose centrifuge mother liquor.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202223322843.2U CN218910202U (en) | 2022-12-11 | 2022-12-11 | System for coproducing xylose crystals and caramel pigment by utilizing xylose massecuite |
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| CN202223322843.2U CN218910202U (en) | 2022-12-11 | 2022-12-11 | System for coproducing xylose crystals and caramel pigment by utilizing xylose massecuite |
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