阅读说明：本技术 NaY分子筛的合成装置及NaY分子筛的合成方法 (NaY molecular sieve synthesis device and NaY molecular sieve synthesis method ) 是由 杨柳 梁维军 卢辉 蒋飞华 李小琴 李军 袁海亮 于 2019-10-31 设计创作，主要内容包括：本发明涉及NaY型分子筛合成领域,公开了一种NaY分子筛的合成装置及NaY分子筛的合成方法。该装置包括：依次连接的反应釜(1)、缓冲釜(2)和晶化釜(3),所述反应釜(1)包括：设置于反应釜(1)内部的第一搅拌器(4)以及设置于反应釜(1)顶部的多根进料管线和设置于反应釜(1)底部的放料管线(5)；其中,所述多根进料管线用于向反应釜(1)中加入合成NaY分子筛的不同反应原料。本发明的装置能够实现反应的连续合成以及连续进出料,从而实现成胶过程的全连续化生产。(The invention relates to the field of synthesis of NaY type molecular sieves, and discloses a synthesis device and a synthesis method of a NaY molecular sieve. The device includes: reation kettle (1), buffer kettle (2) and crystallization kettle (3) that connect gradually, reation kettle (1) includes: the device comprises a first stirrer (4) arranged in a reaction kettle (1), a plurality of feeding pipelines arranged at the top of the reaction kettle (1) and a discharging pipeline (5) arranged at the bottom of the reaction kettle (1); wherein the plurality of feed lines are used for adding different reaction raw materials for synthesizing the NaY molecular sieve into the reaction kettle (1). The device can realize the continuous synthesis of reaction and continuous feeding and discharging, thereby realizing the full-continuous production in the gelling process.)

1. The utility model provides a synthesizer of NaY molecular sieve, the device is including reation kettle (1), buffer kettle (2) and crystallization kettle (3) that connect gradually, its characterized in that, reation kettle (1) includes:

the device comprises a first stirrer (4) arranged in a reaction kettle (1), a plurality of feeding pipelines arranged at the top of the reaction kettle (1) and a discharging pipeline (5) arranged at the bottom of the reaction kettle (1);

wherein the plurality of feed lines are used for adding different reaction raw materials for synthesizing the NaY molecular sieve into the reaction kettle (1).

2. The NaY molecular sieve synthesizer of claim 1, characterized in that the reaction kettle (1) is connected with an overflow line (6).

3. The NaY molecular sieve synthesizer of claim 1, characterized in that an overflow trough (7) is provided in the reaction kettle (1).

4. The apparatus for synthesizing NaY molecular sieve according to any one of claims 1-3, wherein the plurality of feed lines is 6.

5. The apparatus for synthesizing NaY molecular sieve according to claim 4, wherein a flow meter is respectively arranged on the plurality of feeding pipelines.

6. The apparatus for synthesizing NaY molecular sieve according to claim 4, wherein the plurality of feeding lines are respectively provided with a regulating valve.

7. The NaY molecular sieve synthesizer of claim 1, characterized in that a second stirrer (21) is arranged in the buffer tank (2).

8. The NaY molecular sieve synthesizer of claim 1, characterized in that a third stirrer (31) is arranged in the crystallization kettle (3).

9. A method for synthesizing NaY molecular sieve, which comprises the following steps:

1) adding reaction raw materials into the reaction kettle through a plurality of feeding pipelines simultaneously to carry out reaction;

2) and (2) buffering and crystallizing the gel product generated in the step 1) to obtain the NaY molecular sieve.

10. The method for synthesizing NaY molecular sieve according to claim 9, wherein the reaction raw materials comprise: water glass, silica-alumina gel, a guiding agent, sodium metaaluminate, aluminum sulfate and water.

Technical Field

The invention relates to the field of molecular sieve preparation, in particular to a synthesis device and a synthesis method of a NaY molecular sieve.

Background

The production process and engineering research of the Y-type molecular sieve as the active component of the FCC catalyst are always the research hotspots of various overseas large catalyst manufacturers and engineering companies. In recent years, these large catalyst manufacturing enterprises have made major breakthroughs in some key technologies through reintegration and merging of research institutions, and have formed multiple proprietary technologies and are still in a confidential state. In China, the research on engineering technology is started later.

At present, the colloid-forming reaction process of the NaY type molecular sieve at home and abroad is still a chemical process of batch reaction, and is generally carried out in a stirring reaction kettle in stages. The method mainly comprises the steps of sequentially feeding and mixing water glass, a guiding agent, aluminum sulfate, low-alkali sodium metaaluminate and silica-alumina gel and the like. During the addition, a white gum is formed, the pH of the slurry gradually decreases, and the viscosity increases. When the pH value of the material reaches a certain value, a thick point is formed, the viscosity of the material reaches a maximum value at the moment, the power of a stirring motor is increased sharply, and the stirring efficiency is reduced greatly. The materials are agglomerated and blocky. With the further addition of the raw materials, the pH value is gradually increased, the viscosity is gradually reduced, and the large-grained materials are gradually reduced, but the homogenization of the materials is difficult to realize within the time range allowed by industrial production. On the other hand, batch gelling reaction can be realized only by increasing the volume of the reaction kettle to improve the production capacity because the treatment capacity of the reaction kettle per unit volume is small. Therefore, the motor power of the gelatinizing reaction kettle is increased, the production energy consumption is increased, the flow dead zone is increased due to the increase of the volume in the large gelatinizing reaction kettle, the mixing effect is reduced, and the product quality is influenced.

Therefore, it is urgently needed to provide a method for continuously preparing the NaY type molecular sieve.

Disclosure of Invention

The invention aims to overcome the problems in the prior art and provides a NaY molecular sieve synthesis device and a NaY molecular sieve synthesis method, wherein the device can realize continuous synthesis of reaction and continuous feeding and discharging, so that full-continuous production in a gelling process is realized.

In order to achieve the above object, one aspect of the present invention provides a NaY molecular sieve synthesizing apparatus, which includes a reaction kettle, a buffer kettle and a crystallization kettle, which are connected in sequence, wherein the reaction kettle includes:

the first stirrer is arranged in the reaction kettle, and the plurality of feeding pipelines are arranged at the top of the reaction kettle and the discharging pipeline is arranged at the bottom of the reaction kettle;

wherein, the plurality of feed lines are used for adding different reaction raw materials for synthesizing the NaY molecular sieve into the reaction kettle.

Preferably, an overflow line is connected to the reaction kettle.

Preferably, an overflow groove is arranged in the reaction kettle.

Preferably, the plurality of feed lines is 6.

Preferably, a flow meter is respectively arranged on the plurality of feeding pipelines.

Preferably, the plurality of feed pipes are respectively provided with a regulating valve.

Preferably, a second stirrer is arranged in the buffer kettle.

Preferably, a third stirrer is arranged in the crystallization kettle.

The second aspect of the invention provides a method for synthesizing NaY molecular sieve, which adopts the NaY molecular sieve synthesizing device of the invention, and comprises the following steps:

1) adding reaction raw materials into the reaction kettle through a plurality of feeding pipelines simultaneously to carry out reaction;

2) and (2) buffering and crystallizing the gel product generated in the step 1) to obtain the NaY molecular sieve.

Preferably, the reaction raw materials comprise: water glass, silica-alumina gel, a guiding agent, sodium metaaluminate, aluminum sulfate and water.

Compared with the prior art, the invention has the following beneficial effects:

1) the continuity and the automation are realized, the labor intensity of workers is reduced, and the production efficiency is improved;

2) the continuous reaction is realized, so that the volume of the reaction kettle is greatly reduced, the stirring efficiency is greatly improved, the dispersion and the reaction of materials are facilitated, and the unit volume processing capacity is further improved;

3) the colloid viscosity is small in the gelling process, the reaction time is further shortened, and the stirring energy consumption is reduced.

Drawings

FIG. 1 is a schematic structural diagram of a NaY molecular sieve synthesizing device according to a preferred embodiment of the present invention;

FIG. 2 is a schematic diagram showing the overall structure of a NaY molecular sieve synthesizing device according to a preferred embodiment of the present invention;

FIG. 3 is a schematic flow chart of the method for synthesizing the NaY molecular sieve of the invention.

Description of the reference numerals

1. Reaction kettle 4 and first stirrer

11. A first feed line 111, a first flow meter 112, a first regulating valve

12. Second feed line 121, second flow meter 122, second regulator valve

13. A third feed line 131, a third flow meter 132, a third regulating valve

14. A fourth feed line 141, a fourth flow meter 142, a fourth regulating valve

15. Fifth feed line 151, fifth flow meter 152, fifth regulating valve

16. Sixth feed line 161, sixth flow meter 162, sixth regulating valve

2. Buffer tank 21 and second stirrer

3. Crystallization kettle 31 and third stirrer

5. Discharge pipeline 51, first stop valve

6. Overflow line 7, overflow launder

Detailed Description

In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.

Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.

In the description of the embodiments of the present invention, it should be noted that the terms "upper", "inner", and the like refer to orientations or positional relationships based on the orientations or positional relationships shown in the drawings or orientations or positional relationships that are conventionally arranged when the products of the present invention are used, and are used only for convenience in describing the present invention and simplifying the description, but do not indicate or imply that the devices or elements referred to must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.

In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.

In a first aspect, the invention provides a NaY molecular sieve synthesis device, which comprises a reaction kettle 1, a buffer kettle 2 and a crystallization kettle 3, which are connected in sequence, wherein the reaction kettle 1 comprises:

a first stirrer 4 arranged in the reaction kettle 1, a plurality of feeding pipelines arranged at the top of the reaction kettle 1 and a discharging pipeline 5 arranged at the bottom of the reaction kettle 1;

wherein the plurality of feed lines are used for adding different reaction raw materials for synthesizing the NaY molecular sieve into the reaction kettle 1.

According to the invention, different raw materials are simultaneously added into the reaction kettle through different feeding pipelines for reaction, so that the chemical composition, the pH value and the viscosity of the materials are relatively constant in the whole reaction process, the viscosity of the materials is low due to no occurrence of thick spots, the stirring efficiency is improved, the dispersity of the colloid is good in a certain retention time, and the colloid which is completely reacted can be continuously discharged, so that the colloid enters a buffer kettle and a crystallization kettle in the next step to obtain the NaY molecular sieve. The device can effectively solve the problems of dispersion and reaction in the continuous gelling process, and meanwhile, in the device, the material inlet and outlet flow is balanced, the liquid level is stable, and no instrument or electrical element acts, so that no equipment fault exists, and the process is effectively controlled.

In the device, the number of the feeding pipelines is not particularly limited, different raw materials can be fed through different pipelines, in the reaction process of preparing the NaY molecular sieve by adopting water glass, silica-alumina gel, a guiding agent, sodium metaaluminate and aluminum sulfate, the plurality of feeding pipelines can be 5 or 6, when 5 feeding pipelines are adopted, 5 feeding pipelines can simultaneously feed the 5 different reaction raw materials, and water in the reaction process can be fed with any one raw material through the same feeding pipeline; when 6 feed lines are used, the aforementioned 5 raw materials and water may be introduced into reaction tank 1 through different feed lines.

The arrangement of the plurality of feeding lines is not particularly limited, the plurality of feeding lines may be arranged on the same side of the reaction vessel 1, or different lines may be arranged on different sides, for example, the first, second and third feeding lines may be distributed on the same side of the reaction vessel 1, the fourth, fifth and sixth feeding lines may be distributed on the other side of the continuous gel-forming reaction vessel, or other different manners and combinations may be adopted, and the raw materials introduced into the feeding lines are not particularly limited.

In order to ensure continuous reaction without generating a thick spot and to control the raw material, in the apparatus of the present invention, it is preferable that a flow meter is provided on each of the plurality of feed lines.

In the device of the invention, a plurality of feeding pipelines can be controlled by a flowmeter and a regulating valve DCS in a centralized way. The invention realizes the full continuous production of the gelling process by adding the required liquid raw materials for synthesizing NaY into the continuous synthesis reaction kettle through the metering, control and parallel flow of the flowmeter and the regulating valve, and continuously feeding and discharging materials.

In order to further ensure the continuous reaction without generating a thick spot and to control the raw material, in the apparatus of the present invention, it is preferable that the plurality of feed lines are respectively provided with a control valve. Realize controlling each raw materials that lets in reation kettle 1 through above-mentioned flowmeter and governing valve, further guaranteed whole reaction process, the chemical composition of material, pH value and viscosity are invariable relatively, the thick point does not appear to guarantee the low viscosity of material, improve stirring efficiency, in certain dwell time, make the dispersibility of colloid good, realize the continuous ejection of compact through the blowing pipeline 5 that sets up in the bottom simultaneously, guaranteed going on in succession of whole production process.

As shown in fig. 1, a reaction kettle 1, a buffer kettle 2 and a crystallization kettle 3 are sequentially connected, a first stirrer 4 is arranged in the reaction kettle 1, 6 feeding pipelines 11-16 are arranged at the top of the reaction kettle 1, different reaction raw materials are introduced into the reaction kettle 1 through 6 feeding pipelines, the reaction is carried out under the stirring of the first stirrer 4, and the generated product is discharged through a discharging pipeline 5 and enters the buffer kettle 2.

In the apparatus of the present invention, preferably, an overflow line 6 is connected to the reaction vessel 1. In the device, top feeding is realized through a feeding pipeline arranged at the top, overflow discharging is adopted, the reaction time and speed are controlled by controlling the feeding volume, the chemical composition, the pH value and the viscosity of the material are not changed along with the change of time (equal pH value and equal viscosity reaction), and the problems of thick spots and the like in batch-process colloid forming are solved.

In the apparatus of the present invention, it is preferable that an overflow tank 7 is provided in the reaction tank 1. In one embodiment of the present invention, isopipe 7 is a U-shaped isopipe. As shown in fig. 1, the U-shaped overflow trough is disposed at the bottom of the reaction vessel 1 and is communicated with the overflow line 6, and the product in the reaction vessel overflows into the buffer vessel 2 through the U-shaped overflow trough and the overflow line 6.

In order to further ensure the uniformity of the product, in the apparatus of the present invention, it is preferable that a second stirrer 21 is provided in the buffer tank 2. As shown in FIG. 2, the discharged product from the reaction vessel 1 is further stirred by a second stirrer 21 and then fed into a crystallization vessel 3.

In order to further ensure the uniformity of the product, in the apparatus of the present invention, it is preferable that a third stirrer 31 is provided in the crystallization kettle 3.

In a second aspect, the present invention further provides a method for synthesizing NaY molecular sieve, which uses the apparatus for synthesizing NaY molecular sieve, and comprises the following steps:

1) adding reaction raw materials into the reaction kettle through a plurality of feeding pipelines simultaneously to carry out reaction;

2) and (2) buffering and crystallizing the gel product generated in the step 1) to obtain the NaY molecular sieve.

According to the method provided by the invention, the reaction raw materials are added into the continuous synthesis reaction kettle in a parallel flow manner through different feeding pipelines, so that the chemical composition, the pH value and the viscosity of the materials are relatively constant in the whole reaction process, no thick point is generated, the low viscosity of the materials is ensured, the stirring efficiency is improved, the dispersibility of the colloid is good in a certain retention time, meanwhile, the continuous feeding and discharging of the materials are realized through the discharging pipelines arranged at the bottom, the full-continuous production in the gelling process is realized, and the continuous operation of the whole production process is ensured.

In the method of the present invention, preferably, the reaction raw materials include: water glass, silica-alumina gel, a guiding agent, sodium metaaluminate, aluminum sulfate and water.

As shown in figure 3, continuous synthesis of the NaY molecular sieve is realized by adding water glass, silica-alumina gel, a directing agent, sodium metaaluminate, aluminum sulfate and water in a concurrent flow manner, and the NaY molecular sieve is obtained after crystallization.

The following is a description of a method for synthesizing NaY using the NaY synthesizing apparatus of the present invention.

As shown in fig. 3, the NaY synthesizing apparatus of the present invention includes: a reaction kettle 1, a buffer kettle 2 and a crystallization kettle 3 which are connected in sequence, a first stirrer 4 is arranged in the reaction kettle 1, first to sixth feeding pipelines 11-16 are arranged at the top of the reaction kettle 1 (the first feeding pipeline 11, the second feeding pipeline 12 and the third feeding pipeline 13 are distributed at the same side of the reaction kettle 1, the fourth feeding pipeline 14, the fifth feeding pipeline 15 and the sixth feeding pipeline 16 are distributed at the other side of the continuous gel-forming reaction kettle, the first feeding pipeline 11 is provided with a first flowmeter 111 and a first regulating valve 112, the second feeding pipeline 12 is provided with a second flowmeter 121 and a first regulating valve 122, the third feeding pipeline 13 is provided with a third flowmeter 131 and a third regulating valve 132, the fourth feeding pipeline 14 is provided with a fourth flowmeter 141 and a fourth regulating valve 142, the fifth feeding pipeline 15 is provided with a fifth flowmeter 151 and a fifth regulating valve 152, the sixth feeding pipeline 16 is provided with a sixth flowmeter 161 and a sixth regulating valve 162), the discharging pipeline 5 is arranged at the bottom of the reaction kettle 1 (the discharging pipeline 5 is provided with a first stop valve 51), the overflow groove 7 (particularly a U-shaped overflow groove) is arranged at the bottom of the reaction kettle 1 and communicated with the overflow pipeline 6, the buffer kettle 2 is internally provided with a second stirrer 21, and the crystallization kettle 3 is internally provided with a third stirrer 31.

Specifically, water glass (SiO) is introduced into the first feed line 11₂Not less than 250g/l, modulus 3.1-3.4), silica-alumina gel is introduced into the second feeding pipeline 12, and guiding agent (in terms of molar ratio, Na) is introduced into the third feeding pipeline 13₂O：SiO₂：Al₂O₃：H₂O is 12-20: 12-20: 1: 300-₂O：Al₂O₃The mass concentration ratio is 1.45-1.55), aluminum sulfate (Al) is introduced into the fifth feeding pipeline 15₂O₃Is 90 +/-2 g/l) and a sixth feeding pipeline 16, adding the 6 reaction raw materials into a reaction kettle 1 at the same time, and reacting under the stirring of a first stirrer 4; and the generated gel product enters a buffer kettle through an overflow pipe 6 and a discharge pipeline 5, is stirred by a second stirrer 21 and then is pumped into a crystallization kettle 3, and is crystallized under the stirring of a third stirrer to generate the NaY molecular sieve.

Preparation example 1

535.3g of water glass (SiO) was added to the beaker₂255.0g/L of high alkalinity sodium metaaluminate solution (Al), 1.250 of specific gravity and 3.27 of modulus₂O₃The content of Na is 40.90g/L₂O content 276.8g/L, specific gravity 1.322) and 121.8g deionized water, and aging at 25 deg.C for 18 hr to obtain 16Na₂O∶Al₂O₃∶15SiO₂∶320H₂A directing agent for O.

Example 1

Water glass (specific gravity 1.261, SiO) was fed into the first feed line 11 at room temperature of 25 ℃ at a rate of 94.02L/min₂259.4g/L, modulus 3.40), 86.46L/min for the second feed line 12, 28.1L/min for the diverting agent synthesized in preparation example 1 for the third feed line 13, 15.01L/min for the sodium metaaluminate solution (Al) for the fourth feed line 14₂O₃The content of Na is 190.4g/L₂O content 289.9g/L, specific gravity 1.408), and aluminum sulfate solution (Al) is fed into the fifth feed line 15 at a rate of 20.94L/min₂O₃91.50g/L, a specific gravity of 1.287), and 24.26L/based on the total weight of the sample in the sixth feed line 16Deionized water is introduced at the speed of min, and the reaction is carried out under the stirring of the first stirrer 4; the generated gel product enters a buffer kettle 2 through an overflow pipe 6, is stirred by a second stirrer 21, is pumped to a crystallization kettle 3, and is stirred by a third stirrer and then is kept stand at 100 ℃ for crystallization to generate the NaY molecular sieve.

The gel formed in the above reaction vessel 1 was: pH12.5, molar ratio of 2.77Na₂O∶Al₂O₃∶8.4SiO₂∶209H₂And (3) taking the NaY molecular sieve generated in the crystallization kettle for O gel, and detecting the NaY molecular sieve by using a scanning electron microscope, wherein the complete XRD characteristic peak of the crystal grain crystal form of the NaY molecular sieve is matched with the Y molecular sieve.

Example 2

Water glass (specific gravity 1.261, SiO) was fed into the first feed line 11 at room temperature of 25 ℃ at a rate of 107L/min₂259.4g/L, modulus 3.40), 113.18L/min for the second feed line 12, 33.72L/min for the directing agent synthesized in preparation example 1 for the third feed line 13, 17.36L/min for the sodium metaaluminate solution (Al) for the fourth feed line 14₂O₃The content of Na is 190.4g/L₂O content 289.9g/L, specific gravity 1.408), and aluminum sulfate solution (Al) was fed into the fifth feed line 15 at a rate of 22.55L/min₂O₃91.50g/L, 1.287 specific gravity), deionized water is fed into the sixth feeding line 16 at a rate of 29.1L/min, and the reaction is carried out under the stirring of the first stirrer 4; the generated gel product enters a buffer kettle 2 through an overflow pipe 6, is stirred by a second stirrer 21, is pumped to a crystallization kettle 3, and is stirred by a third stirrer and then is kept stand at 100 ℃ for crystallization to generate the NaY molecular sieve.

The gel formed in the above reaction vessel 1 was: pH12.5, molar ratio of 2.77Na₂O∶Al₂O₃∶8.4SiO₂∶209H₂And (3) taking the NaY molecular sieve generated in the crystallization kettle for O gel, and detecting the NaY molecular sieve by using a scanning electron microscope, wherein the complete XRD characteristic peak of the crystal grain crystal form of the NaY molecular sieve is matched with the Y molecular sieve.

Example 3

At room temperature of 25 ℃ at 128.37L/min in the first feed line 11Water glass (specific gravity 1.261, SiO) is introduced at a speed₂259.4g/L, modulus 3.40), feeding silica-alumina gel at 78.6L/min into the second feed line 12, feeding the directing agent synthesized in preparation example 1 at 33.72L/min into the third feed line 13, and feeding the sodium metaaluminate solution (Al) at 19.74L/min into the fourth feed line 14₂O₃The content of Na is 190.4g/L₂289.9g/L O content, 1.408 specific gravity), and aluminum sulfate solution (Al) is fed into the fifth feed line 15 at 32.03L/min₂O₃91.50g/L, 1.287 specific gravity), deionized water is fed into the sixth feeding line 16 at a rate of 29.14L/min, and the reaction is carried out under the stirring of the first stirrer 4; the generated gel product enters a buffer kettle 2 through an overflow pipe 6, is stirred by a second stirrer 21, is pumped to a crystallization kettle 3, and is stirred by a third stirrer and then is kept stand at 100 ℃ for crystallization to generate the NaY molecular sieve.

The gel formed in the above reaction vessel 1 was: pH12.5, molar ratio of 2.77Na₂O∶Al₂O₃∶8.4SiO₂∶209H₂And (3) taking the NaY molecular sieve generated in the crystallization kettle for O gel, and detecting the NaY molecular sieve by using a scanning electron microscope, wherein the complete XRD characteristic peak of the crystal grain crystal form of the NaY molecular sieve is matched with the Y molecular sieve.

The NaY molecular sieve synthesized by the device provided by the invention can realize continuity and automation, greatly reduce the labor intensity of workers and improve the production efficiency; by adopting a continuous reaction mode, the volume of the reaction kettle can be greatly reduced, the stirring efficiency is greatly improved, the dispersion and the reaction of materials are facilitated, and the unit volume processing capacity of the reaction kettle is about 10 times that of an intermittent reaction kettle; because the colloid viscosity is small in the colloid forming process, the reaction time is short, and the stirring energy consumption is reduced by more than 80% compared with that in the batch process.

The preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention. Including each of the specific features, are combined in any suitable manner. The invention is not described in detail in order to avoid unnecessary repetition. Such simple modifications and combinations should be considered within the scope of the present disclosure as well.