CN212491640U - Crystallization device for co-production of sodium sulfite - Google Patents
Crystallization device for co-production of sodium sulfite Download PDFInfo
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- CN212491640U CN212491640U CN202021005937.5U CN202021005937U CN212491640U CN 212491640 U CN212491640 U CN 212491640U CN 202021005937 U CN202021005937 U CN 202021005937U CN 212491640 U CN212491640 U CN 212491640U
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Abstract
The invention discloses a crystallization device for co-producing sodium sulfite, which comprises a separation chamber, a connecting rod, a flow guide pipe, a stirring paddle and a stirrer motor, wherein the separation chamber is provided with a separation chamber; the guide pipe is nested on the connecting rod and is concentric with the central axis of the connecting rod; the stirrer motor is connected with the connecting rod and drives the stirring paddle to stir through the connecting rod, and the stirring paddle is close to the bottom of the separation chamber; the connecting rod is arranged in the center of the separation chamber; a circulating feed inlet and a circulating discharge outlet are formed in the side surface of the separation chamber; a heater and a circulating pump are arranged on a pipeline connecting the circulating feed inlet and the circulating discharge outlet; the material is discharged from the circulating discharge hole, sequentially passes through the circulating pump and the heater, and then enters the separation chamber again through the circulating feed hole. Large particles in the circulating slurry are easy to settle to the bottom of the separation chamber under the dual actions of inertia force and self gravity during the operation of the device, and the separation chamber is provided with the stirring paddle, so that the process requirement of intermittent use is met.
Description
Technical Field
The utility model relates to a chemical industry and environmental protection field specifically are a crystallization device of joint production sodium sulfite.
Background
The slurry can continuously and slowly generate toxic pollution due to oxidation, impurity ions brought by raw materials and the like in the production of sodium metabisulfite, the process cannot be avoided, the regeneration of the slurry or the regular replacement of the slurry is a way for ensuring that the product has more economic advantages, and the co-production of sodium metabisulfite is one of the most common and best economic technologies in the industry. Based on the particularity of the physical property characteristics of the sodium sulfite prepared from the sodium metabisulfite slurry, the conventional evaporative crystallization device has low applicability, and a better recommended process is not seen in professional literature.
The single-effect evaporation system or the multi-effect evaporation system which is commonly adopted in the industry has high comprehensive energy consumption and large wastewater yield during the use.
Patent CN201720313391.1 provides a reactor for preparing sodium sulfite from sulfur dioxide in tail gas, which adopts a cyclone separation mode, and can not avoid the objective problems described above.
Patent CN201210429319.7 discloses a process for evaporation concentration of sodium sulfite solution, which is a continuous operation system, and has low steam consumption and poor adaptability to batch production.
Therefore, it is necessary to develop a new crystallization device for co-producing sodium sulfite, which can effectively reduce the density of the circulating liquid, reduce the risk of blocking pipelines and equipment, and reduce the civil engineering cost.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to provide a reduce circulation liquid density, reduce the jam risk of pipeline, equipment, reduce civil engineering cost's the crystallization device of coproduction sodium sulfite.
In order to solve the technical problem, the technical proposal adopted by the utility model is that the crystallization device for co-producing sodium sulfite comprises a separation chamber, a connecting rod, a flow guide pipe, a stirring paddle and a stirrer motor;
the honeycomb duct is nested on the connecting rod and is concentric with the central axis of the connecting rod; the stirrer motor is connected with the connecting rod and drives the stirring paddle to stir through the connecting rod, and the stirring paddle is close to the bottom of the separation chamber;
the connecting rod is arranged in the center of the separation chamber; an exhaust port and a liquid supplementing port are arranged at the upper part of the separation chamber, and a discharge port is arranged at the lower part of the separation chamber;
a circulating feed inlet and a circulating discharge outlet are formed in the side surface of the separation chamber; a heater and a circulating pump are arranged on a pipeline connected with the circulating feed inlet and the circulating discharge outlet; and the material is discharged from the circulating discharge hole, sequentially passes through the circulating pump and the heater and then enters the separation chamber again through the circulating feed hole.
The guide pipe also has the function of separating light components from heavy components; large particles in the circulating slurry are easy to settle to the bottom of the separation chamber under the dual actions of inertia force and self gravity, so that the density of the circulating slurry is effectively reduced, and the blocking risk of pipelines and equipment is reduced; the side surface of the separation chamber is provided with a circulating feed inlet and a circulating discharge outlet, so that the separation chamber can be arranged on the ground, and the civil engineering cost is reduced; meanwhile, the separation chamber is provided with a stirring paddle, so that the process requirement of intermittent use is met.
Preferably, the separation chamber is a cylinder, and the top of the separation chamber is in a convex end socket shape.
Preferably, the paddle is an anchor paddle, which does not disturb the slurry, but merely serves to prevent hardening of the crystal precipitate.
Preferably, the height of the vertical section of the stirring paddle is not less than 10cm, and the wall surface of the lower part of the container is scaled; the stirring paddle with the wall interval of separation chamber is 1 ~ 50cm, can cause the wall scale deposit too far away, too closely, and the stirring paddle can increase and produce the friction risk with the wall, increases links such as equipment preparation, installation in the technological cost of precision.
Preferably, the distance between the stirring paddle and the wall surface of the separation chamber is 3-5 cm.
Preferably, the ratio of the horizontal cross sectional area of the lowest part of the vertical section of the draft tube to the cross sectional area of the separation chamber on the same horizontal plane is not more than 0.5; the method mainly controls the shallow speed of the fluid, reduces the fluid disturbance, and reduces the proportion of large particles returning to the circulating pump.
Preferably, the lowest part of the vertical section of the flow guide pipe is expanded outwards to form a horn shape, so that the solution speed is reduced, the fluid section is expanded again after the fluid exits from the horn mouth, the solution speed is further reduced, and more sedimentation of large particles is facilitated.
Preferably, the ratio of the horizontal cross-sectional area of the vertical section of the draft tube to the horizontal cross-sectional area of the lowest flared section is no greater than 0.5.
Preferably, the level of the circular discharge hole is higher than that of the lower part of the flow guide pipe, so that fluid with more large particles is prevented from entering circulation.
Preferably, the ratio of liquid-gas ratio of the fluid flowing through the flow guide pipe is controlled to be 0.1-2, and the flow rate of the fluid flowing out of the flow guide pipe is controlled to be 0.1-2 m/s.
Preferably, the flow rate of the fluid out of the draft tube is controlled to be 0.2-0.5 m/s; and the liquid-gas ratio of the fluid flowing through the flow guide pipe is controlled to be 0.2-0.5.
Drawings
The following is a more detailed description of embodiments of the present invention with reference to the accompanying drawings:
FIG. 1 is a schematic view of the overall structure of a crystallization device for co-producing sodium sulfite of the present invention;
wherein: 1-separation chamber, 2-circulation discharge port, 3-connecting rod, 4-discharge port, 5-stirring paddle, 6-guide pipe, 7-circulation feed port, 8-fluid infusion port, 9-exhaust port, 10-stirrer motor, 11-circulation pump and 12-heater.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
As shown in fig. 1, the crystallization device for co-producing sodium sulfite of the present invention comprises a separation chamber 1, a connecting rod 3, a draft tube 6, a stirring paddle 5 and a stirrer motor 10;
the honeycomb duct 6 is nested on the connecting rod 3 and is concentric with the central axis of the connecting rod 3; the stirrer motor 10 is connected with the connecting rod 3, and drives the stirring paddle 5 to stir through the connecting rod 3, and the stirring paddle 5 is close to the bottom of the separation chamber 1;
the connecting rod 3 is arranged in the center of the separation chamber 1; an exhaust port 9 and a liquid supplementing port 8 are arranged at the upper part of the separation chamber 1, and a discharge port 4 is arranged at the lower part of the separation chamber 1;
a circulating feed inlet 7 and a circulating discharge outlet 2 are arranged on the side surface of the separation chamber 1; a heater 12 and a circulating pump 11 are arranged on a pipeline connecting the circulating feed inlet 7 and the circulating discharge outlet 2; the material comes out from the circulating discharge hole 2 and sequentially passes through the circulating pump 11 and the heater 12, and then enters the separation chamber 1 again through the circulating feed hole 7.
The separation chamber 1 in the embodiment is a cylinder, and the top of the separation chamber 1 is in a convex end socket shape; the stirring paddle 5 is an anchor type paddle, the height of a vertical section of the stirring paddle 5 is not less than 10cm, and the distance between the stirring paddle 5 and the wall surface of the separation chamber 1 is 1-50 cm; preferably, the distance between the stirring paddle 5 and the wall surface of the separation chamber 1 is 3-5 cm.
The ratio of the horizontal cross sectional area of the lowest part of the vertical section of the draft tube 6 to the cross sectional area of the separation chamber 1 on the same horizontal plane is not more than 0.5; the lowest part of the vertical section of the draft tube 6 expands outwards to form a horn shape; the ratio of the horizontal cross-sectional area of the vertical section of the draft tube 6 to the horizontal cross-sectional area of the lowest flared section is not more than 0.5.
The level of the circulating discharge port 2 is higher than the level of the lower part of the draft tube 6.
The liquid-gas ratio of the fluid flowing through the draft tube 6 is controlled to be 0.1-2, and the flow rate of the fluid out of the draft tube 6 is controlled to be 0.1-2 m/s; preferably, the flow rate of the fluid out of the draft tube 6 is controlled to be 0.2-0.5 m/s; the liquid-gas ratio of the fluid flowing through the draft tube 6 is controlled to be 0.2-0.5.
The process flow comprises the following steps: external slurry (material) enters the separation chamber 1 through the liquid supplementing port 8 and is mixed with the slurry in the separation chamber 1, the slurry circulating discharge port 2 leaves the separation chamber 1 and returns to the separation chamber 1 from the circulating feed port 7 and the guide pipe 6 under the action of the circulating pump 11, the heater 12 and the like, large-particle crystals fall into the bottom of the separation chamber 1 under the action of inertia force and gravity, and smaller particles continue to circulate along with the slurry; the gas collected at the top of the separation chamber 1 leaves the separation chamber 1 through the gas outlet 9 and the slurry at the bottom of the separation chamber 1 exits the separation chamber 1 through the discharge opening 4.
It is noted that, herein, relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (10)
1. A crystallization device for coproducing sodium sulfite is characterized by comprising a separation chamber, a connecting rod, a flow guide pipe, a stirring paddle and a stirrer motor;
the honeycomb duct is nested on the connecting rod and is concentric with the central axis of the connecting rod; the stirrer motor is connected with the connecting rod and drives the stirring paddle to stir through the connecting rod, and the stirring paddle is close to the bottom of the separation chamber;
the connecting rod is arranged in the center of the separation chamber; an exhaust port and a liquid supplementing port are arranged at the upper part of the separation chamber, and a discharge port is arranged at the lower part of the separation chamber;
a circulating feed inlet and a circulating discharge outlet are formed in the side surface of the separation chamber; a heater and a circulating pump are arranged on a pipeline connected with the circulating feed inlet and the circulating discharge outlet; and the material is discharged from the circulating discharge hole, sequentially passes through the circulating pump and the heater and then enters the separation chamber again through the circulating feed hole.
2. The crystallization device for co-producing sodium sulfite according to claim 1, wherein the stirring paddle is an anchor paddle.
3. The crystallization apparatus for co-producing sodium sulfite according to claim 1, wherein the vertical section of the stirring paddle has a height of not less than 10 cm.
4. The crystallization device for co-producing sodium sulfite according to claim 3, wherein the distance between the stirring paddle and the wall surface of the separation chamber is 3-5 cm.
5. The crystallization device for co-producing sodium sulfite according to claim 4, wherein the ratio of the horizontal cross sectional area of the lowest part of the vertical section of the draft tube to the cross sectional area of the separation chamber on the same horizontal plane is not more than 0.5.
6. The crystallization device for co-producing sodium sulfite according to claim 5, wherein the lowest part of the vertical section of the draft tube is flared outwards.
7. The crystallization device for co-producing sodium sulfite according to claim 6, wherein the ratio of the horizontal cross-sectional area of the vertical section of the draft tube to the horizontal cross-sectional area of the lowest part expanded into the bell-mouth shape is not more than 0.5.
8. The crystallization device for co-producing sodium sulfite according to claim 1, wherein the level of the circular discharge port is higher than the level of the lower part of the draft tube.
9. The crystallization device for co-producing sodium sulfite according to any one of claims 1 to 8, wherein the ratio of liquid to gas ratio of the fluid flowing through the flow guide pipe is controlled to be 0.1 to 2, and the flow rate of the fluid flowing out of the flow guide pipe is controlled to be 0.1 to 2 m/s.
10. The crystallization device for co-producing sodium sulfite according to any one of claims 1 to 8, wherein the flow rate of the fluid out of the draft tube is controlled to be 0.2 to 0.5 m/s; and the liquid-gas ratio of the fluid flowing through the flow guide pipe is controlled to be 0.2-0.5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021005937.5U CN212491640U (en) | 2020-06-04 | 2020-06-04 | Crystallization device for co-production of sodium sulfite |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021005937.5U CN212491640U (en) | 2020-06-04 | 2020-06-04 | Crystallization device for co-production of sodium sulfite |
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| Publication Number | Publication Date |
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| CN212491640U true CN212491640U (en) | 2021-02-09 |
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| CN202021005937.5U Active CN212491640U (en) | 2020-06-04 | 2020-06-04 | Crystallization device for co-production of sodium sulfite |
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