A synthetic device for ammonium bromide

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By designing an ammonium bromide synthesis device including ammonization tank and bromide tank, the continuous production and efficient purification of ammonium bromide are achieved by using the continuous input and circulation of ammonia and bromide gas, and the problems of low production efficiency and high cost in the prior art are solved.

CN222739133UActive Publication Date: 2025-04-11SHANDONG HAIWANG CHEM

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Patent Information

Application Number: CN202420598989.X
Authority / Receiving Office: CN · China
Patent Type: Utility models(China)
Current Assignee / Owner
Filing Date: 2024-03-26
Publication Date: 2025-04-11
Estimated Expiration: 2034-03-26

AI Technical Summary

Technical Problem

The existing ammonium bromide production process has problems of low production efficiency and high production costs, especially the redox method adopts intermittent production methods, which leads to large energy consumption.

Method used

A synthesis device of ammonium bromide is designed, including an ammonia tank and a bromide tank. Through continuous input and circulation treatment of ammonia and bromide, the continuous production of ammonia bromide is achieved, and the ammonium bromide crystals are directly obtained through suspension separation and solid-liquid separation of centrifuge, avoiding the evaporation and concentration crystallization process.

Benefits of technology

The continuous production of ammonium bromide is achieved, production efficiency is improved, energy costs are saved, and the obtained solid-phase ammonium bromide does not require further evaporation and concentration, which is environmentally friendly and efficient.

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Abstract

The utility model discloses a synthesis device of ammonium bromide, and relates to the technical field of ammonium bromide production. An ammonia gas inlet pipeline is connected to an ammonia tank, a bromination tank is connected to a bromine gas inlet pipeline, a bottom outlet of the ammonia tank is connected to a first circulation pump through a pipeline, an outlet of the first circulation pump is connected to a first suspension separator through a pipeline, and a solid phase outlet of the first suspension separator is connected to a buffer tank through a pipeline; a bottom outlet of the bromination tank is connected to a second circulation pump through a pipeline, an outlet of the second circulation pump is connected to a second suspension separator through a pipeline, and a solid phase outlet of the second suspension separator is connected to the buffer tank through a pipeline, and the ammonia tank and the bromination tank are connected through an overflow pipeline; an outlet of the buffer tank is connected to a centrifuge through a pipeline, and a solid phase outlet of the centrifuge is connected to an ammonium bromide crystal discharge pipeline. Continuous feeding is realized, production efficiency is improved, and the obtained solid phase ammonium bromide does not need evaporation, concentration and crystallization, energy costs are saved, and it is environmentally friendly.

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Description

Technical Field

[0001] The utility model relates to the technical field of ammonium bromide production, in particular to a synthesis device for ammonium bromide. Background Art

[0002] At present, the production process of ammonium bromide mainly includes three methods: neutralization method, double decomposition method, and oxidation-reduction method. The neutralization method uses ammonia water and hydrobromic acid as raw materials, and the two undergo a neutralization reaction to produce ammonium bromide products. The reaction formula is: NH3˙H2O+HBr→NH4Br+H2O ①

[0003] The double decomposition method uses iron bromide (or calcium bromide) and ammonia (or ammonium carbonate) to undergo double decomposition reaction to generate ammonium bromide. The reaction formula is: FeBr3+3NH3·H2O→3NH4Br+Fe(OH)3↓ ②

[0004] CaBr2+(NH4)2CO3→2NH4Br+CaC03↓ ③

[0005] The redox method uses bromine and ammonia as raw materials, and the two undergo redox reaction to produce ammonium bromide products. The reaction formula is: 8NH3·H20+3Br2→6NH4Br+N2↑+8H20

[0006] Among them, the redox method often adopts an intermittent production method, which has low production efficiency, and the obtained crude ammonium bromide needs to be further evaporated, concentrated and crystallized to obtain a crystalline product, which has high production costs. Summary of the invention

[0007] The technical problem to be solved by the utility model is: in view of the shortcomings of the prior art, a synthesis device of ammonium bromide is provided, which realizes continuous production and saves energy consumption during evaporation and high production cost.

[0008] In order to solve the above technical problems, the technical solution of the utility model is:

[0009] An ammonium bromide synthesis device comprises an ammoniation tank and a bromination tank, wherein the ammoniation tank is connected to an ammonia gas inlet pipeline, the bromination tank is connected to a bromine gas inlet pipeline, the bottom outlet of the ammoniation tank is connected to a first circulation pump through a pipeline, the outlet of the first circulation pump is connected to a first suspension separator through a pipeline, and the solid phase outlet of the first suspension separator is connected to a buffer tank through a pipeline;

[0010] The bottom outlet of the bromination tank is connected to a second circulation pump through a pipeline, the outlet of the second circulation pump is connected to a second suspension separator through a pipeline, the solid phase outlet of the second suspension separator is connected to the buffer tank through a pipeline, and the amination tank and the bromination tank are connected through an overflow pipeline;

[0011] The outlet of the buffer tank is connected to a centrifuge through a pipeline, and the solid phase outlet of the centrifuge is connected to an ammonium bromide crystal discharge pipeline.

[0012] As an improved technical solution, the ammoniazing tank is connected to a deionized water inlet pipeline.

[0013] As an improved technical solution, a first venturi tube is provided at the inlet of the ammonia tank, the gas phase inlet of the first venturi tube is connected to the ammonia gas inlet pipeline, and the liquid phase outlet of the first suspension separator is connected to the liquid phase inlet of the first venturi tube through a pipeline.

[0014] As an improved technical solution, a second venturi tube is provided at the inlet of the bromination tank, the gas phase inlet of the second venturi tube is connected to the bromine gas inlet pipeline, and the liquid phase outlet of the second suspension separator is connected to the liquid phase inlet of the second venturi tube through a pipeline.

[0015] As an improved technical solution, the liquid phase outlet of the second suspension separator is connected to the upper inlet of the bromination tank through a pipeline.

[0016] As an improved technical solution, the outlet of the second circulation pump is connected to a condenser through a pipeline, and the outlet of the condenser is connected to the second suspension separator through a pipeline.

[0017] As a preferred technical solution, the mother liquor outlet of the centrifuge is connected to the upper inlet of the bromination tank through a pipeline.

[0018] As a preferred technical solution, the ammonia tank is provided with a pH sensor, the ammonia gas inlet pipeline is provided with an automatic regulating valve, and the pH sensor and the automatic regulating valve are interlocked to a control system.

[0019] Due to the adoption of the above technical solution, the beneficial effects of the utility model are:

[0020] The utility model discloses an ammonium bromide synthesis device, comprising an ammonia tank and a bromination tank, wherein the ammonia tank is connected with an ammonia gas inlet pipeline, the bromination tank is connected with a bromine gas inlet pipeline, the bottom outlet of the ammonia tank is connected with a first circulation pump through a pipeline, the outlet of the first circulation pump is connected with a first suspension separator through a pipeline, and the solid phase outlet of the first suspension separator is connected with a buffer tank through a pipeline; the bottom outlet of the bromination tank is connected with a second circulation pump through a pipeline, the outlet of the second circulation pump is connected with a second suspension separator through a pipeline, the solid phase outlet of the second suspension separator is connected to the buffer tank through a pipeline, the ammonia tank and the bromination tank are connected with an overflow pipeline; the outlet of the buffer tank is connected with a centrifuge through a pipeline, and the solid phase outlet of the centrifuge is connected with an ammonium bromide crystal discharge pipeline. Ammonia gas and bromine gas continuously enter the ammoniation tank and the bromination tank, and are connected to each other through an overflow pipe, ammonium bromide is continuously generated in the ammoniation tank and the bromination tank, and then the solid ammonium bromide is discharged into the buffer tank through the first suspension separator and the second suspension separator, and then the solid-liquid separation is performed through a centrifuge to obtain ammonium bromide crystals, thereby realizing continuous feeding and improving production efficiency. The obtained solid-phase ammonium bromide does not need to be evaporated, concentrated and crystallized, thus saving energy costs and being environmentally friendly.

[0021] The ammonia tank of the utility model is connected with a deionized water inlet pipe. The deionized water enters the ammonia tank and enters the bromination tank through the overflow pipe, thus achieving the balance of the liquid levels in the ammonia tank and the bromination tank.

[0022] The inlet of the ammoniation tank is provided with a first venturi tube, the gas phase inlet of the first venturi tube is connected to the ammonia gas inlet pipeline, and the liquid phase outlet of the first suspension separator is connected to the liquid phase inlet of the first venturi tube through a pipeline. The negative pressure generated when the liquid phase obtained by the first suspension separator enters the ammoniation tank can draw in ammonia and mix it, so that the mixing effect of the materials in the ammoniation tank is better, the conversion rate of ammonia is improved, and the yield of ammonium bromide is higher.

[0023] The inlet of the bromination tank is provided with a second venturi tube, the gas phase inlet of the second venturi tube is connected to the bromine gas inlet pipeline, and the liquid phase outlet of the second suspension separator is connected to the liquid phase inlet of the second venturi tube through a pipeline. The negative pressure generated when the liquid phase obtained by the second suspension separator enters the bromination tank can draw in and mix the bromine gas, so that the mixing effect of the materials in the bromination tank is better, the conversion rate of the bromine gas is improved, and the yield of ammonium bromide is higher.

[0024] The liquid phase outlet of the second suspension separator is connected to the upper inlet of the bromination tank through a pipeline. The liquid phase obtained after the material in the bromination tank is separated by the second suspension separator enters the ammonia tank to react with the ammonia gas therein, while the material in the ammonia tank enters the bromination tank through the overflow pipeline, thereby achieving flow mixing of the materials in the two tanks and achieving a better reaction effect.

[0025] The outlet of the second circulating pump is connected to a condenser through a pipeline, and the outlet of the condenser is connected to the second suspension separator through a pipeline. The temperature of the circulating liquid in the bromination tank is maintained at about 40°C through the condenser, and the reaction process is more stable with a high safety factor.

[0026] The mother liquor outlet of the centrifuge is connected to the upper inlet of the bromination tank through a pipeline. By re-introducing the centrifugal mother liquor into the bromination tank for reaction, the waste of raw materials is avoided and the yield of the product is improved.

[0027] The ammonia tank is provided with a pH sensor, the ammonia gas inlet pipeline is provided with an automatic regulating valve, and the pH sensor and the automatic regulating valve are interlocked with a control system. The control system adjusts the opening of the automatic regulating valve according to the value of the pH sensor, so that the pH value of the circulating liquid in the ammonia tank is controlled at 8-10, avoiding safety hazards such as explosion caused by excessive concentration of ammonia water. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] The utility model is further described below in conjunction with the accompanying drawings and embodiments.

[0029] Figure 1 It is a structural schematic diagram of an embodiment of the utility model;

[0030] Among them: 1. ammonia tank; 2. bromination tank; 3. ammonia gas inlet pipeline; 4. bromine gas inlet pipeline; 5. first circulation pump; 6. first suspension separator; 7. buffer tank; 8. second circulation pump; 9. second suspension separator; 10. overflow pipeline; 11. centrifuge; 12. ammonium bromide crystal discharge pipeline; 13. deionized water inlet pipeline; 14. first venturi tube; 15. second venturi tube; 16. condenser; 17. pH sensor; 18. automatic regulating valve. DETAILED DESCRIPTION

[0031] The present invention will be further described below in conjunction with the accompanying drawings and embodiments.

[0032] like Figure 1As shown, a synthesis device of ammonium bromide comprises an ammonia tank 1 and a bromination tank 2, wherein the ammonia tank 1 is connected to an ammonia gas inlet pipeline 3, and the bromination tank 2 is connected to a bromine gas inlet pipeline 4, the bottom outlet of the ammonia tank 1 is connected to a first circulation pump 5 through a pipeline, the outlet of the first circulation pump 5 is connected to a first suspension separator 6 through a pipeline, and the solid phase outlet of the first suspension separator 6 is connected to a buffer tank 7 through a pipeline; the bottom outlet of the bromination tank 2 is connected to a second circulation pump 8 through a pipeline, the outlet of the second circulation pump 8 is connected to a second suspension separator 9 through a pipeline, the solid phase outlet of the second suspension separator 9 is connected to the buffer tank 7 through a pipeline, the ammonia tank 1 and the bromination tank 2 are connected through an overflow pipeline 10; the outlet of the buffer tank 7 is connected to a centrifuge 11 through a pipeline, and the solid phase outlet of the centrifuge 11 is connected to an ammonium bromide crystal discharge pipeline 12. Ammonia gas and bromine gas continuously enter the ammoniation tank 1 and the bromination tank 2, and are connected to each other through the overflow pipe 10, ammonium bromide is continuously generated in the ammoniation tank 1 and the bromination tank 2, and then the solid ammonium bromide is discharged into the buffer tank 7 through the first suspension separator 6 and the second suspension separator 9, and then the solid-liquid separation is performed through the centrifuge 11 to obtain ammonium bromide crystals, thereby realizing continuous feeding and improving production efficiency. The obtained solid phase ammonium bromide does not need to be evaporated, concentrated and crystallized, thus saving energy costs and being environmentally friendly.

[0033] The ammoniation tank 1 is connected to a deionized water inlet pipe 13. The deionized water enters the ammoniation tank 1 and enters the bromination tank 2 through the overflow pipe 10, achieving a balance of the liquid levels in the ammoniation tank 1 and the bromination tank 2.

[0034] The inlet of the ammoniation tank 1 is provided with a first venturi tube 14, the gas phase inlet of the first venturi tube 14 is connected to the ammonia gas inlet pipeline 3, and the liquid phase outlet of the first suspension separator 6 is connected to the liquid phase inlet of the first venturi tube 14 through a pipeline. The negative pressure generated when the liquid phase obtained by the first suspension separator 6 enters the ammoniation tank 1 can draw in ammonia and mix it, so that the mixing effect of the materials in the ammoniation tank 1 is better, the conversion rate of ammonia is improved, and the yield of ammonium bromide is higher.

[0035] The inlet of the bromination tank 2 is provided with a second venturi tube 15, the gas phase inlet of the second venturi tube 15 is connected to the bromine gas inlet pipeline 4, and the liquid phase outlet of the second suspension separator 9 is connected to the liquid phase inlet of the second venturi tube 15 through a pipeline. The negative pressure generated when the liquid phase obtained by the second suspension separator 9 enters the bromination tank 2 can draw in the bromination gas and mix it, so that the mixing effect of the materials in the bromination tank 2 is better, the conversion rate of the bromine gas is improved, and the yield of ammonium bromide is higher.

[0036] The liquid phase outlet of the second suspension separator 9 is connected to the upper inlet of the bromination tank 2 through a pipeline. The liquid phase obtained after the material in the bromination tank 2 is separated by the second suspension separator 9 enters the ammonia tank 1 to react with the ammonia gas therein, while the material in the ammonia tank 1 enters the bromination tank 2 through the overflow pipe 10, thereby achieving the flow mixing of the materials in the two tanks and achieving a better reaction effect.

[0037] The outlet of the second circulating pump 8 is connected to a condenser 16 through a pipeline, and the outlet of the condenser 16 is connected to the second suspension separator 9 through a pipeline. The temperature of the circulating liquid in the bromination tank 2 is maintained at about 40° C. by the condenser 16, and the reaction process is more stable with a high safety factor.

[0038] The mother liquor outlet of the centrifuge 11 is connected to the upper inlet of the bromination tank 2 through a pipeline. By reintroducing the centrifuged mother liquor into the bromination tank 2 for reaction, the waste of raw materials is avoided and the yield of the product is improved.

[0039] The ammonia tank 1 is provided with a pH sensor 17, and the ammonia gas inlet pipeline 3 is provided with an automatic regulating valve 18, and the pH sensor 17 and the automatic regulating valve 18 are interlocked with a control system. The control system adjusts the opening of the automatic regulating valve 18 according to the value of the pH sensor 17, so that the pH value of the circulating liquid in the ammonia tank 1 is controlled at 8-10, avoiding safety hazards such as explosion caused by excessive concentration of ammonia water.

[0040] The working principle of this utility model:

[0041] 1. Add deionized water to 50% of the volume of the ammoniation tank 1 and the bromination tank 2 respectively;

[0042] 2. Start the first circulation pump 5 and the second circulation pump 8 to establish circulation;

[0043] 3. Open the ammonia extraction valve, and the ammonia gas enters the ammoniation tank 1 along with the liquid phase separated by the first suspension separator 6. Adjust the opening of the automatic regulating valve 18 to control the pH value of the circulating liquid in the ammoniation tank 1 to 8-10;

[0044] 4. Open the bromine extraction valve, and the bromine gas enters the bromination tank 2 along with the liquid phase separated by the second suspension separator 9, and adjusts

[0045] Control the size of bromine gas intake, control the color of the circulating liquid in the bromination tank 2 to be slightly yellow, and keep the temperature of the circulating liquid in the bromination tank 2 below 40°C;

[0046] 6. When the ammonium bromide slurry in the buffer tank 7 reaches 60% liquid level, the centrifuge 11 is turned on for centrifugal operation;

[0047] 7. The ammonium bromide crystals after centrifugation are collected for subsequent drying, while the centrifuged mother liquor is refluxed to the bromination tank 2 for reuse.

[0048] It should be understood that these embodiments are only used to illustrate the present invention and are not used to limit the scope of the present invention. In addition, it should be understood that after reading the content taught by the present invention, those skilled in the art can make various changes or modifications to the present invention, and these equivalent forms also fall within the scope defined by the claims attached to this application.

Claims

1. A synthesis device for ammonium bromide, characterized in that: It comprises an ammonia tank and a bromination tank, wherein the ammonia tank is connected to an ammonia gas inlet pipeline, the bromination tank is connected to a bromine gas inlet pipeline, the bottom outlet of the ammonia tank is connected to a first circulation pump through a pipeline, the outlet of the first circulation pump is connected to a first suspension separator through a pipeline, and the solid phase outlet of the first suspension separator is connected to a buffer tank through a pipeline; The bottom outlet of the bromination tank is connected to a second circulation pump through a pipeline, the outlet of the second circulation pump is connected to a second suspension separator through a pipeline, the solid phase outlet of the second suspension separator is connected to the buffer tank through a pipeline, and the amination tank and the bromination tank are connected through an overflow pipeline; The outlet of the buffer tank is connected to a centrifuge through a pipeline, and the solid phase outlet of the centrifuge is connected to an ammonium bromide crystal discharge pipeline.

2. A synthetic device for ammonium bromide as claimed in claim 1, characterized in that: The ammoniaizing tank is connected with a deionized water inlet pipeline.

3. A synthetic device for ammonium bromide as claimed in claim 1, characterized in that: The inlet of the ammonia tank is provided with a first venturi tube, the gas phase inlet of the first venturi tube is connected to the ammonia gas inlet pipeline, and the liquid phase outlet of the first suspension separator is connected to the liquid phase inlet of the first venturi tube through a pipeline.

4. A synthetic device for ammonium bromide as claimed in claim 1, characterized in that: The inlet of the bromination tank is provided with a second venturi tube, the gas phase inlet of the second venturi tube is connected to the bromine gas inlet pipeline, and the liquid phase outlet of the second suspension separator is connected to the liquid phase inlet of the second venturi tube through a pipeline.

5. A synthetic device for ammonium bromide as claimed in claim 4, characterized in that: The liquid phase outlet of the second suspension separator is connected to the upper inlet of the bromination tank through a pipeline.

6. A synthetic device for ammonium bromide as claimed in claim 1, characterized in that: The outlet of the second circulation pump is connected to a condenser through a pipeline, and the outlet of the condenser is connected to the second suspension separator through a pipeline.

7. A synthetic device for ammonium bromide as claimed in claim 1, characterized in that: The mother liquor outlet of the centrifuge is connected to the upper inlet of the bromination tank through a pipeline.

8. A synthetic device for ammonium bromide as claimed in claim 1, characterized in that: The ammonia tank is provided with a pH sensor, the ammonia gas inlet pipeline is provided with an automatic regulating valve, and the pH sensor and the automatic regulating valve are interlocked to a control system.