阅读说明：本技术 一种细粉状安赛蜜的结晶方法 (Crystallization method of fine powder acesulfame potassium ) 是由 陈永旭 杨峰宝 刘刚 于 2020-11-30 设计创作，主要内容包括：本发明涉及一种细粉状安赛蜜的结晶方法,包括现有以下装置：脱色煮料釜、粗滤机、精滤机、预冷釜、冷冻釜、精制离心机；其特征在于：(1)将安赛蜜粗品配置成浓度为880-1000g/L的溶液,升温溶解,过滤后进入预冷釜；(2)物料进入预冷釜后,待温度降至70-75℃,将物料过至冷冻釜；(3)物料过至冷冻釜后,将冷冻釜搅拌转速调至33-35HZ,20-30分钟后将冷冻釜盐水阀门打开,物料降温至15-20℃,物料离心分离烘干。本发明优点：通过调整原有工艺的相关操作参数来降低安赛蜜结晶的粒度,减少了每批返工的物料,节约大量成本；原有安赛蜜结晶：20—40目颗粒占比为51.7%,40—100目颗粒占比为48.3%；本发明生产的安赛蜜结晶：20—40目颗粒占比为21.6%,40—100目颗粒占比为78.4%。(The invention relates to a crystallization method of fine powder acesulfame potassium, which comprises the following devices: a decoloration boiling kettle, a coarse filter, a fine filter, a precooling kettle, a freezing kettle and a refining centrifuge; the method is characterized in that: (1) preparing the crude acesulfame potassium into a solution with the concentration of 880-1000g/L, heating to dissolve, filtering and then entering a precooling kettle; (2) after the materials enter a precooling kettle, the temperature is reduced to 70-75 ℃, and the materials are put into a freezing kettle; (3) after the materials pass through the freezing kettle, the stirring speed of the freezing kettle is adjusted to 33-35HZ, after 20-30 minutes, a brine valve of the freezing kettle is opened, the materials are cooled to 15-20 ℃, and the materials are centrifugally separated and dried. The invention has the advantages that: the granularity of acesulfame potassium crystals is reduced by adjusting related operating parameters of the original process, the reworked materials of each batch are reduced, and a large amount of cost is saved; crystallizing the original acesulfame potassium: the proportion of 20-40 mesh particles is 51.7 percent, and the proportion of 40-100 mesh particles is 48.3 percent; the acesulfame crystal produced by the invention comprises the following components: the proportion of 20-40 mesh particles is 21.6%, and the proportion of 40-100 mesh particles is 78.4%.)

1. A crystallization method of fine powder acesulfame potassium comprises the following existing devices: a decoloration boiling kettle, a coarse filter, a fine filter, a precooling kettle, a freezing kettle and a refining centrifuge; the method is characterized by comprising the following steps:

(1) firstly, preparing a crude acesulfame potassium into a solution with the concentration of 880-1000g/L, heating until the solution material is dissolved, and filtering and then entering a precooling kettle;

(2) after the materials enter a precooling kettle, the materials are put into a freezing kettle after the temperature is reduced to 70-75 ℃;

(3) after the materials pass through the freezing kettle, the stirring speed of the freezing kettle is adjusted to 33-35HZ, after 20-30 minutes, a brine valve of the freezing kettle is opened, the materials are cooled to 15-20 ℃, and the materials are centrifugally separated and dried to obtain fine powder acesulfame potassium crystals.

2. The method for crystallizing fine powdery acesulfame k according to claim 1, wherein: the crude acesulfame potassium in the step (1) is prepared into a solution with the concentration of 900-950 g/L.

Technical Field

The invention belongs to the technical field of acesulfame potassium production, and relates to a crystallization method of fine powder acesulfame potassium.

Background

Acesulfame K (AK sugar) is a food additive, can increase the sweet taste of food, has good taste and no calorie, is not metabolized and absorbed in human body, and is an ideal sweetener for middle-aged and elderly people, obese patients and diabetic patients.

In the decoloration and fine-crystallization working section of acesulfame potassium, a certain amount of heavy sugar (obtained by recrystallizing crude sugar after secondary concentration of sugar water) is generally added into a decoloration boiling material kettle, decoloration mother liquor (obtained after refining and centrifugation) is added according to a certain solid-to-liquid ratio, and finally activated carbon is added in proportion, and a decoloration circulating pump and steam are started to carry out decoloration boiling material operation; and after the decoloration and boiling materials are finished, the materials are pumped into a coarse filter for filtering, the filtered filtrate is pumped into a fine filter at a fine finishing section for filtering, the filtered filtrate enters a pre-cooling kettle and a freezing kettle for stepped cooling after being filtered, and after the cooling is finished, centrifugal separation and drying are carried out to obtain a semi-finished product.

In the current production, the produced material particles are large (the particles with the particle diameters of 20-40 meshes account for 50-55 percent, and the particles with the particle diameters of 40-100 meshes account for 45-50 percent), most of the particles do not meet the requirements of customers on the material particle size (the particles with the particle diameters of 20-40 meshes are lower than 20 percent required by the customers), the mesh number required by the customers is further sieved out in the current production, and the rest acesulfame potassium crystals which do not meet the requirements of the customers are put into a decoloring workshop section again for rework, so that a large amount of waste is caused.

Disclosure of Invention

The invention aims to provide a crystallization method of fine powder acesulfame potassium for producing fine powder acesulfame potassium required by customers.

In order to achieve the purpose, the technical scheme adopted by the invention is as follows:

a crystallization method of fine powder acesulfame potassium comprises the following existing devices: a decoloration boiling kettle, a coarse filter, a fine filter, a precooling kettle, a freezing kettle and a refining centrifuge; the method is characterized by comprising the following steps:

(1) firstly, preparing a crude acesulfame potassium (a heavy section) into a solution with the concentration of 880-1000g/L, heating until the solution material is dissolved, and filtering and then entering a precooling kettle;

the concentration of the crude acesulfame potassium is higher than 1000g/L, and the pipeline is easy to be blocked by the materials; when the concentration is lower than 880 g/L, the material is obvious in particle shape;

(2) after the materials enter a precooling kettle, the materials are put into a freezing kettle after the temperature is reduced to 70-75 ℃;

the temperature of the precooling kettle is adjusted to 70-75 ℃ from the original 40-50 ℃, the fineness of the material can be obviously improved, but if the temperature exceeds 75 ℃, the material is easy to block the freezing kettle;

(3) after the materials pass through a freezing kettle, stirring and rotating the freezing kettle to 33-35HZ, opening a brine valve of the freezing kettle after 20-30 minutes, cooling the materials to 15-20 ℃, and centrifugally separating and drying the materials to obtain fine powder acesulfame potassium crystals;

the stirring speed of the freezing kettle is adjusted to 33-35HZ from the original 25HZ, so that the materials can be better scattered, but the materials are not splashed due to too high rotating speed, and therefore a sight glass is influenced and observation is influenced.

Further, the crude acesulfame potassium (in the heavy knot section) in the step (1) is prepared into a solution with the concentration of 900-950 g/L.

The invention has the advantages that: the method reduces the granularity of the acesulfame potassium crystal by adjusting relevant operating parameters (concentration, temperature, rotating speed and the like) of the prior process, reduces materials reworked in each batch, and saves a large amount of cost; crystallizing the original acesulfame potassium: 50-55% of 20-40 mesh particles and 45-50% of 40-100 mesh particles; the acesulfame crystal produced by the invention comprises the following components: 20-40 mesh particles account for 20-25%, and 40-100 mesh particles account for 75-80%.

Drawings

FIG. 1 is a schematic diagram of a fine powder acesulfame potassium crystallization process according to the present invention;

FIG. 2 is a diagram of fine powdered acesulfame potassium particles produced by the present invention;

FIG. 3 is a graph of acesulfame potassium granules produced by the original process.

Detailed Description

Example 1

(1) Putting 2200kg of heavy sugar, 2.5m of decolorization mother liquor and 5kg of active carbon into a decolorization material boiling kettle, starting decolorization stirring and steam to decolorize and boil the materials, wherein the steam pressure is 0.15 MPa; boiling the material to 85 ℃, closing a steam valve, starting a decoloring material beating pump to pump the material into a coarse filter and a fine filter in sequence for filtering, and feeding the filtered material into a precooling kettle;

(2) after the materials enter the pre-cooling kettle, opening a water circulating valve of the pre-cooling kettle to cool the materials, when the temperature is reduced to 75 ℃, allowing the materials to pass through the freezing kettle, and adjusting the stirring speed of the freezing kettle to 33 HZ;

(3) after the materials enter a freezing kettle for 30min, a brine valve of the freezing kettle is opened to cool the materials, and when the temperature of the materials is reduced to 15 ℃, the materials are sent to a refining centrifuge for centrifugal separation and drying to obtain fine powder acesulfame potassium crystal particles (the proportion of 20-40 meshes of particles is 24.7%, and the proportion of 40-100 meshes of particles is 75.3%).

Example 2

(1) Putting 2400kg of heavy sugar, 2.7m of decolorization mother liquor and 5kg of activated carbon into a decolorization material boiling kettle, starting decolorization stirring and steam to decolorize and boil materials, wherein the steam pressure is 0.18 MPa; boiling the material to 92 ℃, closing a steam valve, starting a decoloring material beating pump to pump the material into a coarse filter and a fine filter in sequence for filtering, and feeding the filtered material into a precooling kettle;

(2) after the materials enter the pre-cooling kettle, opening a water circulating valve of the pre-cooling kettle to cool the materials, when the temperature is reduced to 73 ℃, allowing the materials to pass through the freezing kettle, and adjusting the stirring speed of the freezing kettle to 35 HZ;

(3) after the materials enter a freezing kettle for 25min, a brine valve of the freezing kettle is opened to cool the materials, and when the temperature of the materials is reduced to 18 ℃, the materials are sent to a refining centrifuge for centrifugal separation and drying to obtain fine powder acesulfame potassium crystal particles (the proportion of 20-40 mesh particles is 21.6%, and the proportion of 40-100 particles is 78.4%).

Comparative example 1

(1) Putting 1800kg of heavy sugar, 2.5m of decolorization mother liquor and 5kg of active carbon into a decolorization material boiling kettle, starting decolorization stirring and steam to decolorize and boil materials, wherein the steam pressure is 0.15 MPa; boiling the material to 85 ℃, closing a steam valve, starting a decoloring material beating pump to pump the material into a coarse filter and a fine filter in sequence for filtering, and feeding the filtered material into a precooling kettle;

(2) after the materials enter the pre-cooling kettle, opening a water circulating valve of the pre-cooling kettle to cool the materials, when the temperature is reduced to 52 ℃, allowing the materials to pass through the freezing kettle, and adjusting the stirring speed of the freezing kettle to 25 HZ;

(3) after the materials enter a freezing kettle for 30min, a brine valve of the freezing kettle is opened to cool the materials, and when the temperature of the materials is reduced to 15 ℃, the materials are sent to a refining centrifuge for centrifugal separation and drying to obtain granular acesulfame potassium crystal particles (the proportion of 20-40 meshes of particles is 50.3%, and the proportion of 40-100 particles is 49.7%).