CN218854062U

CN218854062U - beta-D-glucose production system

Info

Publication number: CN218854062U
Application number: CN202223212781.XU
Authority: CN
Inventors: 赵六弟; 钱炜雯; 刘永超
Original assignee: Wugan Pharmaceutical Suzhou Co ltd
Current assignee: Wugan Pharmaceutical Suzhou Co ltd
Priority date: 2022-11-30
Filing date: 2022-11-30
Publication date: 2023-04-14
Anticipated expiration: 2032-11-30

Abstract

The utility model relates to a production system of beta-D-glucose, it includes: a dissolving tank; the decoloring filter is connected with the bottom of the dissolving tank through a first pipeline; the top of the concentration tank is connected with the decolorizing filter through a second pipeline; the crystallization treatment device comprises a concentration crystallization tank connected with the bottom of the concentration tank through a third pipeline, a centrifugal machine connected with the bottom of the concentration crystallization tank through a fourth pipeline and a dryer matched with the centrifugal machine; and (4) an induced crystallization device. The concentration tank is connected with the induced crystallization device with a specific structure, so that a small amount of concentrated solution in the concentration tank can be taken for induced crystallization to obtain beta-phase crystal seeds with required specifications, and then the beta-phase crystal seeds are input into the crystallization treatment device for concentrated crystallization to obtain required beta-D-glucose, and the purity of the beta-D-glucose is favorably improved.

Description

beta-D-glucose production system

Technical Field

The utility model belongs to the field of chemical industry equipment, a production system of glucose is related to, concretely relates to production system of beta-D-glucose.

Background

beta-D (+) -glucose means that the hydroxyl group formed by the reaction of the hydroxyl group and the aldehyde group is on the same side of the ring as the hydroxymethyl group, and is alpha-type on the opposite side of the ring. At present, the preparation process of beta-D-glucose mainly comprises the steps of dissolving monohydrate glucose, decoloring/removing impurities, adding seed crystals after concentration to perform concentration crystallization, centrifuging and drying, so that a beta-D-glucose production system correspondingly comprises a dissolving tank, a decoloring filter, a concentration tank, a crystallizing tank, a centrifuge and a dryer which are matched, and the purity and yield of the beta-D-glucose are influenced because the seed crystals are not accurately classified in the process of adding the seed crystals to perform the concentration crystallization.

Disclosure of Invention

The utility model aims to overcome the defects of the prior art and provide a beta-D-glucose production system.

In order to achieve the above purpose, the utility model adopts the technical scheme that: a system for producing β -D-glucose, comprising:

a dissolving tank;

the decoloring filter is connected with the bottom of the dissolving tank through a first pipeline;

the top of the concentration tank is connected with the decoloring filter through a second pipeline;

the crystallization treatment device comprises a concentration crystallization tank connected with the bottom of the concentration tank through a third pipeline, a centrifugal machine connected with the bottom of the concentration crystallization tank through a fourth pipeline and a dryer matched with the centrifugal machine;

the induced crystallization device comprises a material distribution tank connected with the bottom of the concentration tank through a fifth pipeline, a crystallization tank communicated with the material distribution tank through a sixth pipeline, an ultrasonic induced crystallizer installed on the sixth pipeline, a crystal growing tank communicated with the crystallization tank through a seventh pipeline, and a seed crystal grading separator communicated with the crystal growing tank through an eighth pipeline and the concentration crystallization tank through a ninth pipeline.

Optimally, the top of the dissolving tank is provided with a first feed port, a second feed port and a reflux port, the bottom of the dissolving tank is provided with a first discharge port, the outer wall of the dissolving tank is provided with a first heating jacket, and the dissolving tank is provided with a first stirring structure extending to the inside; the first pipeline is connected with the first discharge hole.

Furthermore, a third feeding port and a first steam outlet are formed in the top of the concentration tank, a second discharging port and a third discharging port are formed in the bottom of the concentration tank, a second heating jacket is formed on the outer wall of the concentration tank, a second stirring structure extending to the inside is installed on the second heating jacket, and the first steam outlet is communicated with the backflow port through a first backflow pipe.

Optimally, a first material conveying pump is installed on the second pipeline.

Optimally, the crystallization tank is provided with a polarimeter.

Furthermore, a fourth feed port, a fifth feed port and a second steam outlet are formed in the top of the concentration crystallization tank, a crystallization discharge port is formed in the bottom of the concentration crystallization tank, a third heating jacket is formed on the outer wall of the concentration crystallization tank, a third stirring structure extending to the inside is installed on the third heating jacket, the seed crystal grading separator is communicated with the fifth feed port through a ninth pipeline, and the second steam outlet is communicated with the reflux port through a second reflux pipe.

Because of the application of the technical scheme, compared with the prior art, the utility model has the following advantages: the utility model discloses beta-D-glucose's production system, through the induced crystallization device who connects specific structure on concentrated jar, can get a small amount of concentrate in the concentrated jar like this and induce the crystallization in order to obtain the beta looks seed crystal of required specification, carry out the concentrated crystallization and obtain required beta-D-glucose in the reentrant crystallization processing apparatus (being used for accepting remaining concentrate and carrying out intensive mixing with it and seed crystal), be favorable to improving the purity of beta-D-glucose.

Drawings

FIG. 1 is a schematic structural diagram of a system for producing beta-D-glucose according to the present invention.

Detailed Description

The invention will be further described with reference to examples of embodiments shown in the drawings.

As shown in FIG. 1, the system for producing beta-D-glucose mainly comprises a dissolving tank 1, a decolorizing filter 2, a concentrating tank 3, an induced crystallization device, a crystallization treatment device 9 and the like.

Wherein, the top of the dissolving tank 1 is provided with a first feed inlet 11, a second feed inlet 12 and a return port 13, the bottom is provided with a first discharge outlet 14, the outer wall of the dissolving tank is provided with a first heating jacket 16 (the first heating jacket 16 plays a role of heating or heat preservation), and the dissolving tank is also provided with a first stirring structure 15 (the existing conventional method is adopted, and only the glucose monohydrate is ensured to be dissolved uniformly); specifically, the first feed port 11 is a solid material inlet and is a glucose monohydrate feed port; the second feed port 12 is an inlet for the solvent and a feed port for purified water; the heated purified water can be directly added, or the normal temperature purified water can be added and then heated to the required temperature (60-90 ℃) by utilizing the first heating jacket 16; the first discharge port 14 is a discharge port for an aqueous glucose solution, and the mass concentration thereof reaches 70 to 75 percent.

The decolorizing filter 2 is connected with the bottom of the dissolving tank 1 through a first pipeline, and specifically, the first pipeline is connected with a first discharge hole 14; the glucose aqueous solution is decolorized and purified by the decolorizing filter 2. The decolorizing filter 2 is conventional.

The top of the concentration tank 3 is connected with the decolorizing filter 2 through a second pipeline and is used for receiving the decolorized and impurity-removed glucose aqueous solution and continuously increasing the mass concentration (to 75-80%). In this embodiment, a first material delivery pump 21 is installed on the second pipeline for pumping the decolorized and impurity-removed glucose aqueous solution into the concentration tank 3. Concentrated jar 3 also adopts current conventional can, if the top of concentrated jar 3 has seted up third feed inlet 31 (being glucose aqueous solution pan feeding mouth) and first steam outlet 32 (be used for leading out the vapor in the concentrated jar 3), its bottom is provided with second discharge gate 33 (main discharge gate) and third discharge gate 34 (vice discharge gate, the load of vice discharge gate only accounts for 1 ~ 5% of material quality in the concentrated jar 3), be formed with second heating jacket 35 on its outer wall (can be used for promoting the temperature of material in the concentrated jar 3 or keep warm), it still installs the second stirring structure 36 that extends to inside (adopt current conventional can). The first steam outlet 32 is connected to the return port 13 through a first return pipe, so that high-temperature steam can be recovered and utilized to dissolve dextrose monohydrate, thereby saving energy and improving the utilization rate of purified water.

The crystallization treatment device 9 comprises a concentration crystallization tank 91 connected with the bottom of the concentration tank 3 through a third pipeline, a centrifuge 92 connected with the bottom of the concentration crystallization tank 91 through a fourth pipeline, and a dryer 93 matched with the centrifuge 92. In this embodiment, the concentration and crystallization tank 91 may be conventional, for example, the top of the concentration and crystallization tank 91 is provided with a fourth feeding hole 911 (the fourth feeding hole 911 is connected to the bottom of the concentration tank 3 through a third pipeline, specifically, connected to the second discharging hole 33, and is used for receiving the material in the concentration tank 3), a fifth feeding hole 913 (the fifth feeding hole 913 is used for receiving the β -phase seed crystal formed by the ultrasonic induced crystallization), and a second steam outlet 912 (which is used for guiding out the water vapor in the concentration and crystallization tank 91), the bottom of the concentration and crystallization tank is provided with a crystallization discharging hole 916 for outputting the crystallized material downstream, the outer wall of the concentration and crystallization tank is provided with a third heating jacket 915 (which may be used for raising the temperature of the material in the concentration and crystallization tank 91 or preserving the heat), and the concentration and crystallization tank 91 is also provided with a third stirring structure 914 (which may be conventional) extending to the inside. The second steam outlet 912 is connected to the reflux port 13 through a second reflux pipe, which can join with the first reflux pipe and then connect to the reflux port 13, and also to recover and utilize high temperature steam to dissolve monohydrate dextrose, thus saving energy and improving the utilization rate of purified water.

The induced crystallization device comprises a material distribution tank 4 connected with the bottom of a concentration tank 3 through a fifth pipeline (namely, the material distribution tank 4 is connected with a third discharge port 34 at the bottom of the concentration tank 3 through the fifth pipeline and is used for temporarily storing materials taken out of the concentration tank 3), a crystallization tank 5 (used for receiving crystal-containing concentrated liquid obtained through ultrasonic induction) communicated with the material distribution tank 4 through a sixth pipeline, an ultrasonic induced crystallizer 6 installed on the sixth pipeline (the ultrasonic induced crystallizer 6 is used for crystallizing the materials output from the material distribution tank 4, and can be conventional in the prior art; such as a nucleation inducer disclosed in the Chinese utility model with the application number of 201720571402.6), a crystal growing tank 7 (the conventional structure is used for the growth of the crystals) communicated with the crystallization tank 5 through a seventh pipeline, and a crystal seed grading separator 8 (see the specification disclosed in the Chinese patent with the application number of 202111425973.6 for collecting specific beta-phase crystals and crystal seeds which are respectively communicated with the concentration crystallization tank 91 through a ninth pipeline), and the crystal seed grading separator 8 is used for collecting crystal seeds which is used for continuously inputting the crystal seeds into the crystal seed collecting tank 80-collecting crystals in batches, and the crystal seeds are specifically designed according to obtain the crystal seeds which are used for collecting crystals and are continuously input into the crystal seeds and are concentrated liquid crystal seeds with the crystal collecting device according to the specification 30 mu-80. In this embodiment, the crystallization tank 5 is provided with a polarimeter 51 for determining the crystal form of the crystals in the crystal-containing concentrated liquid.

The above embodiments are only for illustrating the technical concept and features of the present invention, and the purpose of the embodiments is to enable those skilled in the art to understand the contents of the present invention and implement the present invention, which cannot limit the protection scope of the present invention. All equivalent changes and modifications made according to the spirit of the present invention should be covered by the protection scope of the present invention.

Claims

1. A system for producing β -D-glucose, comprising:

a dissolving tank (1);

the decoloring filter (2), the decoloring filter (2) is connected with the bottom of the dissolving tank (1) through a first pipeline;

the top of the concentration tank (3) is connected with the decolorizing filter (2) through a second pipeline;

the crystallization treatment device (9) comprises a concentration crystallization tank (91) connected with the bottom of the concentration tank (3) through a third pipeline, a centrifugal machine (92) connected with the bottom of the concentration crystallization tank (91) through a fourth pipeline and a dryer (93) matched with the centrifugal machine (92);

induced crystallization device, induced crystallization device include through the fifth pipeline with concentrated jar (3) the bottom be connected divide material jar (4), through the sixth pipeline with crystallizer (5) that divide material jar (4) to be linked together, install ultrasonic wave induced crystallizer (6) on the sixth pipeline, through the seventh pipeline with growing crystal jar (7) that crystallizer (5) are linked together and respectively through the eighth pipeline with grow crystal jar (7) be linked together and through the ninth pipeline with seed crystal fractional segregator (8) that concentrated crystallizer (91) are linked together.

2. The β -D-glucose production system according to claim 1, wherein: the top of the dissolving tank (1) is provided with a first feeding hole (11), a second feeding hole (12) and a backflow hole (13), the bottom of the dissolving tank is provided with a first discharging hole (14), the outer wall of the dissolving tank is provided with a first heating jacket (16) and a first stirring structure (15) extending to the inside; the first pipeline is connected with the first discharge hole (14).

3. The β -D-glucose production system according to claim 2, wherein: the top of the concentration tank (3) is provided with a third feed port (31) and a first steam outlet (32), the bottom of the concentration tank is provided with a second discharge port (33) and a third discharge port (34), the outer wall of the concentration tank is provided with a second heating jacket (35) and a second stirring structure (36) extending to the inside, and the first steam outlet (32) is communicated with the reflux port (13) through a first reflux pipe.

4. The β -D-glucose production system according to claim 1, wherein: and a first material conveying pump (21) is arranged on the second pipeline.

5. The β -D-glucose production system according to claim 1, wherein: and a polarimeter (51) is arranged on the crystallizing tank (5).

6. The β -D-glucose production system according to claim 2, wherein: the top of the concentration crystallizing tank (91) is provided with a fourth feeding hole (911), a fifth feeding hole (913) and a second steam outlet (912), and the bottom of the concentration crystallizing tank is provided with a crystallization discharging hole (916), a third heating jacket (915) is formed on the outer wall of the concentration crystallizing tank, and a third stirring structure (914) extending to the inside is installed on the third heating jacket, the seed crystal grading separator (8) is communicated with the fifth feeding hole (913) through a ninth pipeline, and the second steam outlet (912) is communicated with the reflux hole (13) through a second reflux pipe.