A high-efficiency refining equipment and process for fructose-glucose syrup

Abstract

The present invention relates to the technical field of light industry and chemical industry biotechnology, and in particular to an efficient refining equipment and process for fructose-glucose syrup. The present invention obtains an efficient refining process for fructose-glucose syrup through the steps of pH adjustment, primary evaporation, sterilization, primary carbon column refining, secondary carbon column refining, filtration, secondary evaporation and the like. By designing the granular carbon column in series between the two-stage evaporation of the double-effect MVR evaporator, an efficient carbon column with a high temperature of 82°C to 88°C and a high concentration feed of 60% to 67% is designed, the refining efficiency of the granular carbon column is improved, the residual odor factors such as product 2-Ap and HMF are reduced, the product color value is reduced, the product quality is improved, and the shelf life is improved; at the same time, the evaporator and sterilization heat are effectively utilized to avoid waste of waste heat discharge, and energy utilization is more sufficient. At the same time, the present invention ensures the efficient and stable operation of the carbon column by customizing the granular carbon column refining equipment, which is suitable for promotion and application.

Description

Technical Field

[0001] The invention relates to the technical field of light industry and chemical industry biotechnology, and in particular to a high-efficiency refining device and process for fructose-glucose syrup. Background Art

[0002] In the production of high fructose corn syrup, odor chemicals such as 2-aminoacetophenone (hereinafter referred to as 2-Ap) and 5-hydroxymethylfurfural (hereinafter referred to as HMF) are produced due to factors such as residual raw materials and auxiliary materials, Maillard reaction, and production process. 2-AP is a trace substance with aromatic activity, which is mainly found in substances such as high fructose corn syrup, white glucose wine, and milk. 2-AP will produce atypical aging (UTA) phenomenon, producing tastes such as mothballs, carpet paint, and alcohol, which seriously affects the flavor of the product. In the production of high fructose corn syrup, activated carbon is usually used to remove odor compounds such as 2-Ap and HMF. The conventional activated carbon odor removal process adopts a single-column fixed bed form, with low persuading BV and low 2-Ap removal efficiency, which leads to problems such as slow production efficiency, uneven syrup quality, and high production costs.

[0003] Therefore, how to develop an efficient carbon column refining process and equipment has become an urgent problem to be solved by technical personnel in this field. Summary of the invention

[0004] In view of the above situation, the technical problem to be solved by the present invention is how to provide a more efficient fructose-glucose syrup refining equipment and process, so as to better improve the quality of syrup and improve the carbon column refining efficiency.

[0005] To achieve the above object, the present invention provides an efficient refining process for fructose-glucose syrup, comprising the following steps:

[0006] (1) pH adjustment: After the F55 fructose solution is refined in the F55 mixed bed, it enters the MVR evaporator treatment tank and uses dilute acid to adjust the pH of the sugar solution to 3.1-4.2;

[0007] (2) Primary evaporation: The sugar solution enters the primary evaporation system of the MVR evaporator, and the concentration of the sugar solution is increased to 60% to 67%;

[0008] (3) Sterilization: The sugar solution is put into the steam sterilization system, and the temperature of the syrup is gradually raised to above 110°C for sterilization. After the sterilization is completed, the sterilized discharge syrup is heat exchanged with the sterilized feed syrup, and the discharge syrup is cooled to 82°C to 88°C;

[0009] (4) Primary carbon column refining: The sugar solution is introduced into the primary granular carbon column from the top at a rate of 1BV to 4BV for refining. The 2-Ap of the sugar solution discharged from the primary carbon column is controlled to be ≤3ppb, HMF ≤30ppm, and color value ≤15IU;

[0010] (5) Secondary carbon column refining: the sugar solution discharged from the primary carbon column is fed into the secondary granular carbon column from the top at a rate of 1BV to 4BV for refining. The sugar solution discharged from the secondary carbon column has 2-Ap≤0.5ppb, HMF≤15ppm, and color value≤12IU;

[0011] (6) Carbon column conversion: When the output of the primary granular carbon column is 2-Ap>3ppb, the primary granular carbon column is stopped for cleaning and regeneration. After the regeneration is completed, it is used as a standby. The secondary granular carbon column is converted to the primary feed, and the original standby granular carbon column is activated as the secondary feed;

[0012] (7) Filtration: The sugar solution obtained in (5) is pumped out using a carbon column discharge pump and passed into a 2000-mesh filter for high-precision filtration.

[0013] (8) Secondary evaporation: The sterilized syrup enters the secondary evaporation system of the MVR evaporator, where the concentration is increased to 76.5% to 77.5%, and is cooled to below 35°C using cooling water before entering the finished product storage tank.

[0014] Furthermore, when adjusting the pH in step (1), the dilute acid solution used is at least one of hydrochloric acid and citric acid, and the concentration of the dilute acid solution is ≤4%.

[0015] Furthermore, the two-stage granular carbon column is connected in series to pass sugar, and the granular carbon column is arranged between the first and second stages of a double-effect MVR evaporator. The temperature of the granular carbon column is 82°C to 88°C, and the concentration of the sugar solution fed to the granular carbon column is 60% to 67%.

[0016] Also provided is an efficient refining device for fructose-glucose syrup, comprising a granular carbon column, characterized in that the granular carbon column is composed of three fixed beds, each of which is provided with a circle of cylindrical distributors at the bottom to ensure uniform output of the sugar solution;

[0017] A layer of quartz sand of 8cm to 15cm is laid on the distributor to prevent the granular activated carbon from escaping;

[0018] The remaining space of the granular carbon column is filled with granular activated carbon for efficient refining of sugar solution.

[0019] Furthermore, a feed port is provided at the top of the granular carbon column, and a baffle plate is provided below the feed port;

[0020] After the sugar solution enters the granular carbon column from the top, it is first washed on the baffle plate due to inertia, and then evenly dispersed on the granular activated carbon, preventing the sugar solution from partially washing away the activated carbon due to gravity. At the same time, it also makes the feed sugar solution more evenly dispersed, thereby improving the refining effect.

[0021] Furthermore, the granular carbon column is provided with connecting pipelines, which include a feed pipeline, a discharge pipeline and a cleaning and regeneration pipeline;

[0022] The feed pipeline is arranged at the top of the carbon column;

[0023] The discharge pipeline is arranged at the bottom of the carbon column;

[0024] The cleaning and regeneration pipeline is arranged at the bottom of the carbon column, below the discharge pipeline;

[0025] Valves are preset on the feed pipeline, the discharge pipeline and the cleaning and regeneration pipeline, and the feed pipeline, the discharge pipeline and the cleaning and regeneration pipeline can be switched in a carousel manner through the valves according to the actual refining or cleaning conditions of the granular carbon column.

[0026] Furthermore, the particle carbon columns are provided in three numbers, correspondingly forming a primary particle carbon column, a secondary particle carbon column and a spare particle carbon column;

[0027] The discharge pipelines at the bottom of the primary granular carbon column, the secondary granular carbon column and the spare granular carbon column form an interconnected structure through branch pipes;

[0028] Before the first-stage granular carbon column is fed and before steam sterilization, a bypass and a corresponding shut-off valve are provided to facilitate isolation during maintenance of the granular carbon column to avoid affecting the use of the double-effect MVR.

[0029] Furthermore, a primary evaporator and a secondary evaporator are correspondingly arranged on both sides of the feed end and the discharge end of the granular carbon column.

[0030] Furthermore, the first-effect evaporator is preset with a feed inlet and two circulation pumps, and the discharge end of the first-stage evaporator is connected to the first-effect discharge pump via a pipeline, and the other end of the first-stage discharge pump is connected to a sterilization mechanism via a pipeline;

[0031] A heat exchanger is preset in the sterilization mechanism, and the discharge end of the sterilization system is connected with the feed pipeline on the carbon column through a pipeline.

[0032] Further, the secondary evaporator is preset with two circulation pumps, the secondary evaporator is preset with a feed port, and the feed port of the secondary evaporator is connected to a filtering mechanism via a pipeline, the secondary evaporator is preset with a discharge port, and the discharge port is connected to a secondary discharge pump via a pipeline, and the other end of the secondary discharge pump is connected to a cooling mechanism via a pipeline;

[0033] The filtering mechanism includes a carbon column discharge pump and a filter. One end of the carbon column discharge pump is connected to the discharge pipeline of the carbon column through a pipeline, and the other end is connected to the filter through a pipeline. The discharge end of the filter is connected to the feed port of the secondary evaporator through a pipeline.

[0034] The discharge end of the cooling mechanism is connected to an external storage tank through a pipeline.

[0035] The beneficial effects of the present invention are:

[0036] 1. The present invention adopts two-stage granular carbon columns in series to pass sugar. The 2-Ap of the first-stage granular carbon column is controlled to ≤3ppb, HMF≤30ppm, and color value≤15IU, and the 2-Ap of the second-stage granular carbon column is controlled to ≤0.5ppb, HMF≤15ppm, and color value≤12IU. The first-stage carbon column mainly plays the role of initial production, and the second-stage carbon column mainly plays the role of refining. The second-stage granular carbon column is mainly switched after the first-stage granular carbon column discharges 2-Ap>3ppb. In this way, the granular carbon will adsorb most of the 2-Ap of the sugar solution during the first-stage refining, and the remaining adsorption capacity will be used for the second-stage refining, and the adsorption capacity of the granular carbon will be fully utilized; at the same time, after the sugar solution is refined in two stages, the product 2-Ap is reduced by 75% to 82%, HMF is reduced by 27% to 38%, and the color value is reduced by 38% to 52%, the product quality is improved, and the product shelf life can be increased by more than 30%.

[0037] 2. After the first stage of evaporation, the concentration of the sugar solution is 60% to 67%; the temperature after sterilization and heat exchange is 82°C to 88°C. The present invention sets the granular carbon column between the two stages of evaporation, so the feed concentration of the first stage carbon column is 60% to 67%, and the feed temperature of the first stage carbon column is 82°C to 88°C. Conventional carbon columns use a single column operation with a concentration of about 42% and a temperature of about 41°C before evaporation and concentration. In contrast, the sugar passing temperature of the carbon column of the present invention is doubled, and the sugar passing concentration is increased by more than 40%. The syrup can be efficiently refined in series at high temperature and high concentration between the two stages of evaporation. At this concentration and temperature, the sugar passing BV number of the secondary carbon column can reach more than 500BV (limited to 2-Ap≤0.5ppb), the sugar passing volume of the carbon column is increased by more than 60%, the production efficiency is increased by more than 60%, and the production cost is reduced by 26% to 35%.

[0038] 3. The high-temperature and high-concentration feed sugar solution of the carbon column of the present invention directly uses the high-temperature and high-concentration sugar solution after the primary evaporation and sterilization heat exchange in the evaporator concentration process, without the need for re-concentration and heating operations, which can save 11kw.h / t sugar to 16kw.h / t sugar of electricity for evaporation and 0.1kg / t sugar to 7kg / t sugar of steam for evaporation, reflecting the practicality and energy-saving nature of the present invention.

[0039] 4. For the syrup preparation process using high-temperature feed sterilization, since the feed is sterilized at high temperature, the temperature of the entire evaporator is high, and part of the heat that is not fully utilized is discharged to the atmosphere through the condenser, resulting in heat waste. The present invention sets the two-stage carbon column after the first-stage evaporation and sterilization heat exchange, and the sterilization waste heat can be used to maintain the high temperature of the carbon column, thereby effectively utilizing the sterilization waste heat, reducing heat waste, and making more full use of energy.

[0040] 5. The carbon column used in the present invention adopts a fixed bed design, and a circle of cylindrical distributors is arranged at the bottom of the fixed bed, which can better ensure the uniform output of the sugar solution. Then a layer of quartz sand of 8cm to 15cm is laid on the distributor, which can effectively prevent the granular activated carbon from running out. A baffle plate is also arranged below the feed port of the carbon column. After the sugar solution enters the carbon column from the top, it first impacts on the baffle plate, and then is evenly dispersed on the granular activated carbon, preventing the sugar solution from partially flushing the activated carbon, and at the same time, the feed sugar solution can be dispersed more evenly, thereby improving the refining effect.

[0041] 6. The present invention fully considers the maintenance of the carbon column and other situations. Before the feeding of the first-level granular carbon column and before steam sterilization, a bypass and a corresponding shut-off valve are provided to better maintain the carbon column and avoid affecting the use of MVR during the maintenance of the carbon column. BRIEF DESCRIPTION OF THE DRAWINGS

[0042] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0043] Figure 1 It is a refining process diagram of a specific embodiment of the present invention;

[0044] Figure 2 is a front view of a granular carbon column device according to a specific embodiment of the present invention;

[0045] Figure 3 It is a top view of a granular carbon column device according to a specific embodiment of the present invention. DETAILED DESCRIPTION

[0046] Embodiments of the present invention are described in detail below, examples of which are shown in the accompanying drawings, and preferably the same or similar reference numerals throughout represent the same or similar elements or elements having the same or similar functions. The embodiments described below with reference to the accompanying drawings are exemplary and are intended to be used to explain the present invention, and should not be construed as limiting the present invention.

[0047] In the description of the present invention, it should be understood that the terms "length", "width", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside" and the like indicate positions or positional relationships based on the positions or positional relationships shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the present invention. In addition, in the description of the present invention, "multiple" means two or more, unless otherwise clearly and specifically defined.

[0048] See also Figures 1 to 3 , an efficient refining process for fructose syrup, comprising the following steps:

[0049] (1) pH adjustment: After the F55 fructose solution is refined in the F55 mixed bed, it enters the MVR evaporator treatment tank and uses dilute acid to adjust the pH of the sugar solution to 3.1-4.2;

[0050] (2) Primary evaporation: The sugar solution enters the primary evaporation system of the MVR evaporator, and the concentration of the sugar solution is increased to 60% to 67%;

[0051] (3) Sterilization: The sugar solution is put into the steam sterilization system, and the temperature of the syrup is gradually raised to above 110°C for sterilization. After the sterilization is completed, the sterilized discharge syrup is heat exchanged with the sterilized feed syrup, and the discharge syrup is cooled to 82°C to 88°C;

[0052] (4) Primary carbon column refining: The sugar solution is introduced into the primary granular carbon column from the top at a rate of 1BV to 4BV for refining. The 2-Ap of the sugar solution discharged from the primary carbon column is controlled to be ≤3ppb, HMF ≤30ppm, and color value ≤15IU;

[0053] (5) Secondary carbon column refining: the sugar solution discharged from the primary carbon column is fed into the secondary granular carbon column from the top at a rate of 1BV to 4BV for refining. The sugar solution discharged from the secondary carbon column has 2-Ap≤0.5ppb, HMF≤15ppm, and color value≤12IU;

[0054] (6) Carbon column conversion: When the output of the primary granular carbon column is 2-Ap>3ppb, the primary granular carbon column is stopped for cleaning and regeneration. After the regeneration is completed, it is used as a standby. The secondary granular carbon column is converted to the primary feed, and the original standby granular carbon column is activated as the secondary feed;

[0055] (7) Filtration: The sugar solution obtained in (5) is pumped out using a carbon column discharge pump and passed into a 2000-mesh filter for high-precision filtration.

[0056] (8) Secondary evaporation: The sterilized syrup enters the secondary evaporation system of the MVR evaporator, where the concentration is increased to 76.5% to 77.5%, and is cooled to below 35°C using cooling water before entering the finished product storage tank.

[0057] Preferably, when adjusting the pH in step (1), the dilute acid solution used is at least one of hydrochloric acid and citric acid, and the concentration of the dilute acid solution is ≤4%.

[0058] Preferably, the two-stage granular carbon column is connected in series to pass sugar, the granular carbon column is arranged between the first and second stages of a double-effect MVR evaporator, the temperature of the granular carbon column is 82°C to 88°C, and the concentration of the sugar solution fed to the granular carbon column is 60% to 67%.

[0059] Also provided is an efficient refining device for fructose-glucose syrup, comprising a granular carbon column, characterized in that the granular carbon column is composed of three fixed beds, each of which is provided with a circle of cylindrical distributors at the bottom to ensure uniform output of the sugar solution;

[0060] A layer of quartz sand of 8cm to 15cm is laid on the distributor to prevent the granular activated carbon from escaping;

[0061] Granular carbon The remaining space is filled with granular activated carbon for efficient refining of sugar solution.

[0062] Preferably, a feed port is provided at the top of the granular carbon column, and a baffle plate is provided below the feed port;

[0063] After the sugar solution enters the granular carbon column from the top, it first impacts on the baffle plate and then is evenly dispersed on the granular activated carbon, preventing the sugar solution from partially breaking open the activated carbon. At the same time, it also makes the feed sugar solution more evenly dispersed, thereby improving the refining effect.

[0064] Preferably, the granular carbon column is provided with connecting pipelines, which include a feed pipeline, a discharge pipeline and a cleaning and regeneration pipeline;

[0065] The feed pipeline is arranged at the top of the carbon column;

[0066] The discharge pipeline is arranged at the bottom of the carbon column;

[0067] The cleaning and regeneration pipeline is arranged at the bottom of the carbon column, below the discharge pipeline;

[0068] Valves are preset on the feed pipeline, the discharge pipeline and the cleaning and regeneration pipeline, and the feed pipeline, the discharge pipeline and the cleaning and regeneration pipeline can be switched through the valves according to the actual refining or cleaning conditions of the granular carbon column.

[0069] Preferably, the particle carbon columns are provided in three numbers, correspondingly forming a primary particle carbon column, a secondary particle carbon column and a spare particle carbon column;

[0070] The discharge pipelines at the bottom of the primary granular carbon column, the secondary granular carbon column and the spare granular carbon column form an interconnected structure through branch pipes;

[0071] Before the first-stage granular carbon column is fed and before steam sterilization, a bypass and a corresponding shut-off valve are provided to facilitate isolation during maintenance of the granular carbon column to avoid affecting the use of the double-effect MVR.

[0072] Preferably, a primary evaporator and a secondary evaporator are provided on both sides of the feed end and the discharge end of the granular carbon column respectively.

[0073] Preferably, the primary evaporator is preset with a feed inlet and two circulation pumps, and the discharge end of the primary evaporator is connected to a primary discharge pump via a pipeline, and the other end of the primary discharge pump is connected to a sterilization mechanism via a pipeline;

[0074] A heat exchanger is preset in the sterilization mechanism, and the discharge end of the sterilization system is connected with the feed pipeline on the carbon column through a pipeline.

[0075] Preferably, the secondary evaporator is preset with two circulation pumps, the secondary evaporator is preset with a feed port, and the feed port of the secondary evaporator is connected to a filtering mechanism via a pipeline, the secondary evaporator is preset with a discharge port, and the discharge port is connected to a secondary discharge pump via a pipeline, and the other end of the secondary discharge pump is connected to a cooling mechanism via a pipeline;

[0076] The filtering mechanism includes a carbon column discharge pump and a filter. One end of the carbon column discharge pump is connected to the discharge pipeline of the carbon column through a pipeline, and the other end is connected to the filter through a pipeline. The discharge end of the filter is connected to the feed port of the secondary evaporator through a pipeline.

[0077] The discharge end of the cooling mechanism is connected to an external storage tank through a pipeline.

[0078] The working principle of the present invention is:

[0079] First, adjust the pH value of the sugar solution to the specified range according to the needs;

[0080] Secondly, the adjusted sugar solution is sent to the MVR evaporator at the feed end of the carbon column through the preset pipeline for the first-stage evaporation process;

[0081] Next, the first-stage discharge pump is started to pump the sugar solution after the first-stage evaporation into the steam sterilization system through the pipeline for sterilization. After the sterilization is completed, the sterilized discharge syrup is heat-exchanged with the sterilized feed syrup through the heat exchange mechanism in the steam sterilization system.

[0082] Next, when the heat exchange is completed, the pipeline valve on the 1# carbon column is opened, and the sugar solution is sent into the 1# carbon column at a specified speed for primary refining treatment;

[0083] Next, when the first-level refining treatment of the sugar solution is completed, the pipeline valve on the 2# carbon column is opened, and the discharged sugar solution in the 1# carbon column is sent to the 2# carbon column at a specified speed for secondary refining treatment;

[0084] Then, the carbon column discharge pump in the filtration mechanism is started to pump the sugar solution after the secondary refining process into the filter for the filtration process;

[0085] Finally, the filtered sugar solution is pumped into the MVR evaporator at the discharge end of the carbon column through a pipeline for secondary evaporation. After the secondary evaporation is completed, the sugar solution is pumped into the cooling system through a pipeline for cooling. After cooling, it is pumped into the external finished product storage tank through the second-effect discharge pump for storage;

[0086] During use, as the amount of excess sugar increases, the adsorption capacity of the granular carbon gradually approaches saturation, the 1# carbon column is deactivated, and the cleaning mechanism is used for cleaning and regeneration. After the regeneration is completed, the 2# granular carbon column is used as a backup, and the originally backup granular carbon column is activated as a secondary feed, thereby realizing the carbon column switching function.

[0087] Example 1

[0088] The production process flow chart of this embodiment is as follows Figure 1 As shown, the equipment manufacturing diagram is as follows Figure 2 and Figure 3 The specific steps are as follows:

[0089] (1) pH adjustment: corn starch is prepared through slurry adjustment, liquefaction, saccharification, filtration, isomerization, ion exchange, chromatography, F55 blending, mixed bed and other processes to obtain F55 fructose solution for use. After the F55 fructose solution is refined in the F55 mixed bed, it enters the MVR evaporator treatment tank and uses 4% dilute hydrochloric acid solution to adjust the pH of the sugar solution to 4.2. The 2-Ap of the sugar solution is detected to be 7.933 ppb, the HMF is 60.57 ppm, and the color value is 22.38.

[0090] (2) Primary evaporation: The sugar solution then enters the primary evaporation system of the MVR evaporator. After two cycles of compression, the concentration of the sugar solution is increased to 60% for discharge.

[0091] (3) Sterilization: After the sugar solution is evaporated in one effect, it enters the high-temperature sterilization system, where high-temperature steam is used to raise the temperature of the syrup to 110°C for sterilization. After sterilization, the 110°C high-temperature syrup enters the cooling heat exchanger to exchange heat with the feed sugar solution, and the temperature of the sugar solution is cooled to 88°C.

[0092] (4) Primary carbon column refining: A circle of cylindrical distributors is set at the bottom of the three carbon columns, and then a layer of quartz sand is evenly spread on the distributor. The quartz sand is laid to a height of 8 cm so that the quartz sand just covers the distributor, and then granular activated carbon is filled in the remaining space. After the carbon column is prepared, it is cleaned with pure water, and then the sterilized sugar solution is transported from the top into the 1# carbon column as the primary carbon column refining. The feed rate is controlled at 1BV by a regulating valve and a flow meter. After the sugar solution enters the top of the carbon column, it first impacts on the baffle plate, and then is evenly dispersed on the granular activated carbon. After the sugar solution fills the 1# carbon column, it is discharged from the bottom. The 2-Ap of the sugar solution discharged from the 1# carbon column was detected to be 0.041, the HMF of the discharge was 12.35ppm, and the color value was 7.59.

[0093] (5) Secondary carbon column refining: The sugar solution discharged from the primary carbon column is then transported from the top to the 2# carbon column for secondary carbon column refining, and the feed rate is controlled at 1BV. After entering the top of the carbon column, the sugar solution first impacts on the baffle plate, and then is evenly dispersed on the granular activated carbon. After the sugar solution fills the 2# carbon column, it is discharged from the bottom. The 2-Ap of the sugar solution discharged from the 2# carbon column is 0.038ppb, the HMF is 10.80ppm, and the color value is 5.24.

[0094] (6) Filtration: The sugar solution is pumped out of the No. 2 carbon column using a carbon column discharge pump and enters a 2000-mesh filter for high-precision filtration.

[0095] (7) Secondary evaporation: After high-precision filtration, the sugar solution then enters the secondary evaporation system, and the discharge concentration is controlled at 77.5%. The secondary discharge syrup is cooled to 35°C using cooling water and then stored in the finished product storage tank. The discharge pH is detected to be 4.4, and the total number of microorganisms detected is 0 / 10g, which meets the use requirements.

[0096] (8) Carbon column switching: The carbon column continues to pass sugar. As the amount of sugar passing increases, the adsorption capacity of the granular carbon gradually approaches saturation, and the 2-Ap, HMF, and color value of the carbon column output will gradually increase. When the carbon column BV is 1118BV, the 2-Ap of the sugar solution discharged from the 1# carbon column is detected to be 3.535ppb, and the 2-Ap of the 2# carbon column output is detected to be 0.186. At this time, by switching the discharge valve at the bottom of the carbon column and the feed valve at the top, the 2# carbon column is switched to the primary carbon column, and the spare carbon column (i.e., the 3# carbon column) is switched to the secondary carbon column, and the sugar passing continues. The switched 1# carbon column is cleaned and regenerated and then used as a backup.

[0097] Example 2

[0098] The production process flow chart of this embodiment is as follows Figure 1 As shown, the equipment manufacturing diagram is as follows Figure 2 and Figure 3 The specific steps are as follows:

[0099] (1) pH adjustment: corn starch is prepared through slurry adjustment, liquefaction, saccharification, filtration, isomerization, ion exchange, chromatography, F55 blending, mixed bed and other processes to obtain F55 fructose solution for use. After the F55 fructose solution is refined in the F55 mixed bed, it enters the MVR evaporator treatment tank and uses 4% dilute hydrochloric acid solution to adjust the pH of the sugar solution to 3.5. The 2-Ap of the sugar solution is 8.159 ppb, the HMF is 57.80 ppm, and the color value is 21.84.

[0100] (2) Primary evaporation: The sugar solution then enters the primary evaporation system of the MVR evaporator. After two cycles of compression, the concentration of the sugar solution is increased to 65% for discharge.

[0101] (3) Sterilization: After the first stage of evaporation, the sugar solution enters the high temperature sterilization system, where the temperature of the sugar solution is raised to 110°C using high temperature steam for sterilization. After sterilization, the 110°C high temperature sugar solution enters the cooling heat exchanger to exchange heat with the feed sugar solution, and the temperature of the sugar solution is cooled to 85°C.

[0102] (4) Primary carbon column refining: A circle of cylindrical distributors is set at the bottom of the three carbon columns, and then a layer of quartz sand is evenly spread on the distributor. The quartz sand paving height is 15 cm so that the quartz sand completely covers the distributor, and then granular activated carbon is filled in the remaining space of the carbon column. After the carbon column is prepared, it is cleaned with pure water, and then the sterilized sugar solution is transported from the top into the 2# carbon column as the primary carbon column refining. The feed rate is controlled at 2BV by a regulating valve and a flow meter. After the sugar solution enters the top of the carbon column, it first impacts on the baffle plate, and then is evenly dispersed on the granular activated carbon. After the sugar solution fills the 2# carbon column, it is discharged from the bottom. The 2-Ap of the sugar solution discharged from the 2# carbon column was detected to be 0.055ppb, the HMF was 11.69ppm, and the color value was 7.11.

[0103] (5) Secondary carbon column refining: The sugar solution discharged from the primary carbon column is then transported from the top to the 3# carbon column for secondary carbon column refining, and the feed rate is controlled at 2BV. After the sugar solution enters the top of the carbon column, it first impacts on the baffle plate and then is evenly dispersed on the granular activated carbon. After the sugar solution fills the 3# carbon column, it is discharged from the bottom. The 2-Ap of the sugar solution discharged from the 3# carbon column is 0.032ppb, the HMF is 9.88ppm, and the color value is 5.09.

[0104] (6) Filtration: After the sugar solution is discharged from the 3# carbon column, it is pumped out using the carbon column discharge pump and enters a 2000 mesh filter for high-precision filtration.

[0105] (7) Secondary evaporation: The syrup after high-precision filtration enters the secondary evaporation system, and the discharge concentration is controlled at 76.8%. The secondary discharge syrup is cooled to 32°C using cooling water and then stored in the finished product storage tank. The discharge pH is detected to be 3.8, and the total number of microorganisms detected is 0 / 10g, which meets the use requirements.

[0106] (8) Switching of carbon columns: The carbon column is continuously sugared. As the amount of sugared carbon increases, the adsorption capacity of the granular carbon gradually approaches saturation, and the 2-Ap, HMF, and color value of the carbon column output will gradually increase. When the carbon column sugared BV is 1079BV, the 2-Ap of the sugar solution output from the 2# carbon column is detected to be 3.681ppb, and the 2-Ap of the output from the 3# carbon column is detected to be 0.199. At this time, by switching the discharge valve at the bottom of the carbon column and the feed valve at the top, the 3# carbon column is switched to the primary carbon column, and the spare carbon column (i.e., the 1# carbon column) is switched to the secondary carbon column, and the sugared carbon column is continuously passed. The switched 2# carbon column is cleaned and regenerated and then used as a backup.

[0107] Example 3

[0108] The production process flow chart of this embodiment is as follows Figure 1 As shown, the equipment manufacturing diagram is as follows Figure 2 The specific steps are as follows:

[0109] (1) pH adjustment: corn starch is prepared through slurry adjustment, liquefaction, saccharification, filtration, isomerization, ion exchange, chromatography, F55 blending, mixed bed and other processes to obtain F55 fructose solution for use. After the F55 fructose solution is refined in the F55 mixed bed, it enters the MVR evaporator treatment tank and uses 4% dilute hydrochloric acid to adjust the pH of the sugar solution to 3.1. The 2-Ap of the sugar solution is 8.457 ppb, the HMF is 62.01 ppm, and the color value is 23.29.

[0110] (2) Primary evaporation: The sugar solution then enters the primary evaporation system of the MVR evaporator. After two cycles of compression, the concentration of the sugar solution is increased to 67% for discharge.

[0111] (3) Sterilization: After the first stage of evaporation, the sugar solution enters the high temperature sterilization system, where the temperature of the sugar solution is raised to 110°C using high temperature steam for sterilization. After sterilization, the 110°C high temperature sugar solution enters the cooling heat exchanger to exchange heat with the feed sugar solution, and the temperature of the sugar solution is cooled to 82°C.

[0112] (4) Primary carbon column refining: The secondary carbon column that is currently passing sugar is switched to the primary carbon column, and then the sterilized sugar solution is transported from the top to the primary carbon column for refining. The feed rate is controlled at 4BV by a regulating valve and a flow meter. After the sugar solution enters the top of the carbon column, it first impacts the baffle plate, and then is evenly dispersed on the granular activated carbon. After the sugar solution fills the primary carbon column, it is discharged from the bottom. The 2-Ap of the sugar solution discharged from the primary carbon column is 0.215ppb, the HMF is 15.68ppm, and the color value is 8.10.

[0113] (5) Secondary carbon column refining: After cleaning and regeneration, the spare carbon column is switched to the secondary carbon column, and the sugar solution is then transported from the top to the secondary carbon column for refining, and the feed rate is controlled at 4BV. After the sugar solution enters the top of the carbon column, it first impacts on the baffle plate, and then is evenly dispersed on the granular activated carbon. After the sugar solution fills the secondary carbon column, it is discharged from the bottom. The 2-Ap of the sugar solution discharged from the secondary carbon column is detected to be 0.04ppb, the HMF is 10.15ppm, and the color value is 6.02.

[0114] (6) Filtration: After the sugar solution is discharged from the secondary carbon column, it is pumped out using a carbon column discharge pump and enters a 2000-mesh filter for high-precision filtration.

[0115] (7) Secondary evaporation: The sugar solution after high-precision filtration is then sent to the secondary evaporation system, and the discharge concentration is controlled at 76.5%. The secondary discharge syrup is cooled to 28°C using cooling water and then sent to the finished product storage tank for storage. The discharge pH is detected to be 3.3, and the total number of microorganisms detected is 0 / 10g, which meets the use requirements.

[0116] (8) Carbon column switching: The carbon column continues to pass sugar. As the amount of sugar passing increases, the adsorption capacity of the granular carbon gradually approaches saturation, and the 2-Ap, HMF, and color value of the carbon column output gradually increase. When the carbon column BV is 1022BV, the 2-Ap of the sugar solution discharged from the first-level carbon column is detected to be 3.567ppb, and the 2-Ap of the sugar solution discharged from the second-level carbon column is detected to be 0.257. At this time, by switching the discharge valve at the bottom of the carbon column and the feed valve at the top, the second-level carbon column is switched to the first-level carbon column, and the spare carbon column is switched to the second-level carbon column, and the sugar passing continues. The switched first-level carbon column is cleaned and regenerated and then used as a spare.

[0117] Comparison table of refined F55 by the method of the present invention and conventional method:

[0118]

[0119] From the above data, it can be seen that when the present invention is used to refine F55, at the same high sugar content, the new carbon output 2-Ap is still less than 0.2ppb, and the regenerated carbon column 2-Ap is less than 0.3ppb. Compared with the conventional method, the carbon column sugar content 2-Ap, HMF and color value of the present invention are much lower than those of the conventional method, and the product quality and the sugar content of the carbon column are greatly improved. At the same time, compared with the conventional method, the present invention uses the high-temperature, high-concentration sugar solution after the first-stage evaporation and sterilization heat exchange in the evaporator concentration process as the feed, the sugar content temperature is doubled, the sugar content is increased by about 40% or more, the production efficiency is higher, the sterilization waste heat is effectively utilized, the heat waste is reduced, the energy utilization is more sufficient, and the production cost is lower.

[0120] What is disclosed above is only a preferred embodiment of the present invention, and it certainly cannot be used to limit the scope of rights of the present invention. Ordinary technicians in this field can understand that all or part of the processes of the above embodiment and equivalent changes made according to the claims of the present invention still fall within the scope of the invention.

Claims

1. An efficient refining process for fructose-glucose syrup, characterized in that: The following steps are involved: (1) pH adjustment: After the F55 fructose solution is refined in the F55 mixed bed, it enters the MVR evaporator treatment tank and uses dilute acid to adjust the pH of the sugar solution to 3.1-4.2; (2) Primary evaporation: The sugar solution enters the primary evaporation system of the double-effect MVR evaporator, and the concentration of the sugar solution is increased to 60% to 67%; (3) Sterilization: The sugar solution is put into the steam sterilization system, and the temperature of the syrup is gradually raised to above 110°C for sterilization. After the sterilization is completed, the sterilized discharge syrup is heat exchanged with the sterilized feed syrup, and the discharge syrup is cooled to 82°C to 88°C; (4) Primary carbon column refining: The sugar solution is introduced into the primary granular carbon column from the top at a rate of 1BV to 4BV for refining. The 2-Ap of the sugar solution discharged from the primary carbon column is controlled to be ≤3ppb, HMF ≤30ppm, and color value ≤15IU; (5) Secondary carbon column refining: the sugar solution discharged from the primary carbon column is fed into the secondary granular carbon column from the top at a rate of 1BV to 4BV for refining. The sugar solution discharged from the secondary carbon column has 2-Ap≤0.5ppb, HMF≤15ppm, and color value≤12IU; (6) Carbon column conversion: When the output of the primary granular carbon column is 2-Ap>3ppb, the primary granular carbon column is deactivated for cleaning and regeneration. After regeneration, it is used as a standby. The secondary granular carbon column is converted into the primary feed, and the original standby granular carbon column is activated as the secondary feed; (7) Filtration: The sugar solution obtained in (5) is pumped out using a carbon column discharge pump and passed into a 2000-mesh filter for high-precision filtration. (8) Secondary evaporation: The sterilized syrup enters the secondary evaporation system of the double-effect MVR evaporator, where the concentration is increased to 76.5% to 77.5%, and is cooled to below 35°C using cooling water before entering the finished product storage tank.

2. The high-efficiency refining process for high fructose corn syrup according to claim 1, characterized in that: When adjusting the pH in step (1), the dilute acid solution used is at least one of hydrochloric acid and citric acid, and the concentration of the dilute acid solution is ≤4%.

3. The high-efficiency refining process for high fructose corn syrup according to claim 1, characterized in that: The two-stage granular carbon column is connected in series to pass sugar. The granular carbon column is set between the first and second stages of a double-effect MVR evaporator. The temperature of the granular carbon column is 82°C to 88°C, and the concentration of the sugar solution fed to the granular carbon column is 60% to 67%.

4. An efficient refining device for fructose-glucose syrup, comprising a granular carbon column, characterized in that: The granular carbon column is composed of three fixed beds, each of which has a circle of cylindrical distributors at the bottom to ensure uniform output of the sugar solution; A layer of quartz sand of 8cm to 15cm is laid on the distributor to prevent the granular activated carbon from escaping; The remaining space of the granular carbon column is filled with granular activated carbon for efficient refining of sugar solution.

5. The high-efficiency refining equipment for high fructose syrup according to claim 4, characterized in that: A feed inlet is provided at the top of the granular carbon column, and a baffle plate is provided below the feed inlet; After the sugar solution enters the granular carbon column from the top, it first impacts on the baffle plate and then is evenly dispersed on the granular activated carbon, preventing the sugar solution from partially breaking open the activated carbon. At the same time, it also makes the feed sugar solution more evenly dispersed, thereby improving the refining effect.

6. The high-efficiency refining equipment for high fructose corn syrup according to claim 4, characterized in that: The granular carbon column is provided with connecting pipelines, which include a feed pipeline, a discharge pipeline and a cleaning and regeneration pipeline; The feed pipeline is arranged at the top of the carbon column; The discharge pipeline is arranged at the bottom of the carbon column; The cleaning and regeneration pipeline is arranged at the bottom of the carbon column, below the discharge pipeline; Valves are preset on the feed pipeline, the discharge pipeline and the cleaning and regeneration pipeline, and the feed pipeline, the discharge pipeline and the cleaning and regeneration pipeline can be switched through the valves according to the actual refining or cleaning conditions of the granular carbon column.

7. The high-efficiency refining equipment for high fructose corn syrup according to claim 4, characterized in that: The particle carbon columns are provided with three, correspondingly forming a primary particle carbon column, a secondary particle carbon column and a spare particle carbon column; The discharge pipelines at the bottom of the primary granular carbon column, the secondary granular carbon column and the spare granular carbon column form an interconnected structure through branch pipes; Before the first-stage granular carbon column is fed and before steam sterilization, a bypass and a corresponding shut-off valve are provided to facilitate isolation during maintenance of the granular carbon column to avoid affecting the use of the double-effect MVR.

8. The high-efficiency refining equipment for fructose-glucose syrup according to any one of claims 4 to 7, characterized in that: A primary evaporator and a secondary evaporator are correspondingly arranged on both sides of the feed end and the discharge end of the granular carbon column.

9. The high-efficiency refining equipment for high fructose corn syrup according to claim 8, characterized in that: The primary evaporator is preset with a feed inlet and two circulation pumps, and the discharge end of the primary evaporator is connected to the primary discharge pump via a pipeline, and the other end of the primary discharge pump is connected to a sterilization mechanism via a pipeline; A heat exchanger is preset in the sterilization mechanism, and the discharge end of the sterilization system is connected with the feed pipeline on the carbon column through a pipeline.

10. The high-efficiency refining equipment for high fructose corn syrup according to claim 8, characterized in that: The secondary evaporator is preset with two circulation pumps, the secondary evaporator is preset with a feed port, and the feed port of the secondary evaporator is connected to a filtering mechanism via a pipeline, the secondary evaporator is preset with a discharge port, and the discharge port is connected to a secondary discharge pump via a pipeline, and the other end of the secondary discharge pump is connected to a cooling mechanism via a pipeline; The filtering mechanism includes a carbon column discharge pump and a filter. One end of the carbon column discharge pump is connected to the discharge pipeline of the carbon column through a pipeline, and the other end is connected to the filter through a pipeline. The discharge end of the filter is connected to the feed port of the secondary evaporator through a pipeline. The discharge end of the cooling mechanism is connected to an external storage tank through a pipeline.

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