Heat balance system for preparing mixed-phase excited gypsum from wet-process phosphoric acid

Abstract

The utility model discloses a heat balance system for preparing mixed-phase excitation gypsum from wet-process phosphoric acid. The heat balance system comprises a special heat exchanger for utilizing heat generated by diluting concentrated sulfuric acid, an extraction device needing to remove heat and a crystal transformation device needing to be heated. The low-temperature washing liquid G is introduced into the tubular reactor to be diluted and mixed with concentrated sulfuric acid to form high-temperature mixed acid H, the high-temperature mixed acid H is introduced into a shell pass of the heat exchanger, the low-temperature filtrate F is shunted and introduced into a tube pass of the heat exchanger, and the low-temperature filtrate F and the high-temperature mixed acid H are subjected to heat exchange through the heat exchanger; at the moment, the high-temperature mixed acid H is cooled to become low-temperature mixed acid H to be supplied to the dihydrate extraction tank, so that heat generated by dilution of concentrated sulfuric acid and washing liquor G can be utilized, the cost generated by energy consumption during production is reduced, and the problems that flash evaporation equipment is adopted for cooling, and the production cost is reduced are solved. And heat generated by sulfuric acid dilution cannot be effectively utilized.

Description

Technical Field

[0001] This utility model relates to a heat balance system for preparing mixed-phase activated gypsum using wet-process phosphoric acid, and belongs to the technical field of wet-process phosphoric acid preparation systems. Background Technology

[0002] In the production of mixed-phase activated gypsum using wet-process phosphoric acid, the dilution process of concentrated sulfuric acid generates heat of dilution. Since the diluted concentrated sulfuric acid needs to be kept at a low temperature when entering the dihydrate extraction tank, the sulfuric acid dilution process needs to be cooled down.

[0003] The existing technology, as disclosed in Chinese Patent Publication No. CN118458715A, can cool down the sulfuric acid by using flash evaporation equipment, but it cannot effectively utilize the heat generated by the dilution of sulfuric acid. Utility Model Content

[0004] To solve the above-mentioned technical problems, this utility model provides a heat balance system for the preparation of mixed-phase activated gypsum using wet phosphoric acid.

[0005] This utility model is achieved through the following technical solution.

[0006] This utility model provides a heat balance system for the preparation of mixed-phase activated gypsum using wet-process phosphoric acid, comprising:

[0007] Heat exchangers that utilize the heat generated from the dilution of concentrated sulfuric acid, dihydrate extraction tanks that require heat removal, and crystallization tanks that require temperature increases.

[0008] It also includes a tubular reactor for diluting concentrated sulfuric acid and a dihydrate extraction tank for extraction; the tubular reactor is connected to the shell-side inlet of a heat exchanger, the tube-side inlet of the heat exchanger is connected to a filter B, the shell-side outlet of the heat exchanger is connected to the dihydrate extraction tank, and the tube-side outlet of the heat exchanger is connected to a crystallization tank.

[0009] The outlet of the two-water extraction tank is connected to filter A.

[0010] The solid phase outlet of filter A is connected to the crystal transfer tank.

[0011] The slurry outlet of the crystallization tank is connected to filter B.

[0012] The outlet of the filtrate F of the filter B is connected to the inlet of the dihydrate extraction tank and the inlet of the tube side of the dedicated heat exchanger, respectively; the outlet of the washing liquid G of the filter B is connected to the inlet of the tubular reactor.

[0013] The beneficial effects of this invention are as follows: Low-temperature washing solution G is introduced into a tubular reactor and diluted and mixed with concentrated sulfuric acid to form a high-temperature mixed acid H. The high-temperature mixed acid H is introduced into the shell side of a heat exchanger, while low-temperature filtrate F is introduced into the tube side of the heat exchanger. The low-temperature filtrate F and the high-temperature mixed acid H exchange heat through the heat exchanger, causing the low-temperature filtrate F to heat up and become a high-temperature filtrate F, which is then supplied to the crystallization tank. At this time, the high-temperature mixed acid H cools down and becomes a low-temperature mixed acid H, which is then supplied to the dihydrate extraction tank. This allows the heat generated by the dilution of concentrated sulfuric acid and washing solution G to be utilized, reducing the cost of energy consumption during production and solving the problem that the heat generated by the dilution of sulfuric acid cannot be effectively utilized when using flash evaporation equipment for cooling. Attached Figure Description

[0014] Figure 1 This is a schematic diagram of the structure of this utility model;

[0015] In the diagram: 1-Dihydrate extraction tank; 2-Filter A; 3-Crystallization tank; 4-Filter B; 5-Tube reactor; 6-Heat exchanger. Detailed Implementation

[0016] The technical solution of this utility model is further described below, but the scope of protection is not limited to what is described.

[0017] like Figure 1 As shown.

[0018] This application discloses a heat balance system for the wet-process phosphoric acid preparation of mixed-phase activated gypsum, comprising:

[0019] The extraction tank 1 is a dihydrate extraction tank capable of extraction. The dihydrate extraction tank 1 is connected to the filter A2. Mineral powder and concentrated sulfuric acid enter the dihydrate extraction tank 1. The tail gas of the dihydrate extraction tank 1 is fed into the tail gas treatment equipment for treatment. The reaction slurry A after treatment in the dihydrate extraction tank 1 enters the filter A2 for filtration. The filter A2 produces a solid phase B.

[0020] Filter A2 is connected to crystal transfer tank 3. The solid phase B of filter A2 is transported to crystal transfer tank 3 and reacts with the high-temperature filtrate F to obtain slurry D.

[0021] The crystallizer 3 is connected to the filter B4. The slurry D is transported to the filter B4 to produce filtrate F and solid phase. The solid phase is passed into washing water to produce solid phase E and washing liquid G.

[0022] Filter B4 is connected to the dihydrate extraction tank 1 and the tubular reactor 5. The low-temperature filtrate F flows into the dihydrate extraction tank 1, and the low-temperature washing liquid G is fed into the tubular reactor 5 and diluted and mixed with concentrated sulfuric acid to form a high-temperature mixed acid H.

[0023] Tubular reactor 5 is connected to heat exchanger 6. Tubular reactor 5 is connected to the shell inlet of heat exchanger 6. Filter B4 is connected to the tube inlet of heat exchanger 6. The shell outlet of heat exchanger 6 is connected to crystal transfer tank 3. The tube outlet of heat exchanger 6 is also connected to crystal transfer tank 3. High-temperature mixed acid H is introduced into the shell side of heat exchanger 6, and low-temperature filtrate F is introduced into the tube side of heat exchanger 6. The low-temperature filtrate F and the high-temperature mixed acid H exchange heat through heat exchanger 6, causing the low-temperature filtrate F to heat up and become high-temperature filtrate F, which is then supplied to crystal transfer tank 3. At this time, the high-temperature mixed acid H cools down and becomes low-temperature mixed acid H, which is then supplied to dihydrate extraction tank 1. This allows the heat generated by the dilution of concentrated sulfuric acid and washing liquid G to be utilized, reducing the cost of energy consumption during production and solving the problem that the heat generated by the dilution of sulfuric acid cannot be effectively utilized when using flash evaporation equipment for cooling.

[0024] The system proposed in this application eliminates the electricity consumption and equipment investment required for flash evaporation. By rebalancing the heat generated during the dilution of concentrated sulfuric acid, it solves the problems of high investment and energy consumption associated with cooling equipment in extraction tank flash evaporation, and also reduces the external heat energy required for heating the crystal transfer tank.

Claims

1. A heat balance system for the wet-process preparation of mixed-phase activated gypsum using phosphoric acid, characterized in that, include: A heat exchanger (6) that utilizes the heat generated by diluting concentrated sulfuric acid, a dihydrate extraction tank (1) that needs to remove heat, and a crystallization tank (3) that needs to be heated; It also includes a tubular reactor (5) for diluting concentrated sulfuric acid and a dihydrate extraction tank (1) for extraction; the tubular reactor (5) is connected to the shell-side inlet of a heat exchanger (6), the tube-side inlet of the heat exchanger (6) is connected to a filter B (4), the shell-side outlet of the heat exchanger (6) is connected to the dihydrate extraction tank (1), and the tube-side outlet of the heat exchanger (6) is connected to a crystallization tank (3). The outlet of the two-water extraction tank (1) is connected to filter A (2).

2. The heat balance system for preparing mixed-phase activated gypsum using wet-process phosphoric acid as described in claim 1, characterized in that: The solid phase outlet of the filter A (2) is connected to the crystal transfer tank (3).

3. The heat balance system for preparing mixed-phase activated gypsum using wet-process phosphoric acid as described in claim 1, characterized in that: The slurry outlet of the crystal transfer tank (3) is connected to the filter B (4).

4. The heat balance system for preparing mixed-phase activated gypsum using wet-process phosphoric acid as described in claim 1, characterized in that: The outlet of the filter B (4) is connected to the inlet of the dihydrate extraction tank (1) and the inlet of the tube side of the special heat exchanger (6); the outlet of the washing liquid G of the filter B (4) is connected to the inlet of the tubular reactor (5).

Images