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Mines, seas and lakes salt brine thermal cycle method ammonia-alkali process

A salt brine and heat cycle technology, applied in the direction of ammonium halide, carbonate preparations, calcium/strontium/barium halides, etc., can solve the problems of waste of resources, large discharge system, poor product quality, etc., to reduce energy consumption and cost, to solve the effect of environmental protection

Active Publication Date: 2018-08-10
CHINA LIGHT IND INT ENG CO LTD +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0002] Known production soda ash process has the Lublan method, ammonia soda method and cold method combined soda ash method, wherein: 1) soda ash produced by the Lublin method: The Lublan method has poor product quality, high production cost, large labor consumption and production Process is all carried out between solid phases, is difficult to the shortcoming such as continuous operation; 2) Solvay process alkali: Solvay process (ammonia soda process) raw material sodium chloride utilization rate is low (the utilization rate of sodium is about 75%, the utilization of chlorine rate of 0%), distillation waste liquid (contains a large amount of calcium chloride, sodium chloride, every production of 1 ton of soda ash produces 9-10m 3 Waste liquid discharge) The discharge system has a huge amount, wasting resources and forming new environmental pollution; 3) Combined legal soda ash (cold method combined soda method): solid sodium chloride needs to be used as raw material, and the cost of raw material is relatively high. Salt-out crystalline ammonium chloride consumes a lot of power, so it cannot directly use mine, sea and lake salt brine as raw material
Therefore, the application of the above-mentioned processes in actual production has limitations.

Method used

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  • Mines, seas and lakes salt brine thermal cycle method ammonia-alkali process

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0026] Embodiment 1: take 100m 3 Raw materials (mineral salt brine) (NaCl 300g / l, NaCl 2 SO 4 15g / l, MgSO 4 0.30g / l, CaSO 4 2.0g / l) and 170m 3 Ammonium making mother liquor (NH 4 Cl 190.6g / l, Na 2 SO 4 9.94g / l, NaCl 220g / l) and 6.34m 3 Reaction of deammonization mother liquor with lime and refining with lime and calcium chloride to remove magnesium and sulfate ions to obtain magnesium hydroxide, calcium sulfate precipitate and sulfur-removing brine, adding soda ash to remove sulfur-removing brine to obtain refined brine and calcium carbonate precipitate 276.34m obtained after refining ore brine 3 Refined brine (NaCl 288g / l, Na 2 SO 4 6.26g / l) and ammonia (NH 3 ), carbon dioxide (CO 2 ) as a raw material for metathesis reaction (reaction temperature 30°C) to separate and obtain 43 tons of solid sodium bicarbonate (NaHCO 3 ) and 276.34m 3 Contains ammonium chloride, sodium chloride and sodium sulfate (NaCl 138g / l, Na 2 SO 4 6.26g / l, NH 4 Cl 220g / l) and amm...

Embodiment 2

[0027] Embodiment 2: take 100m 3 Raw materials (sea salt brine) (NaCl 300g / l, Na 2 SO 4 15g / l, MgSO 4 0.30g / l, CaSO 4 2.0g / l) and 170m 3 Ammonium making mother liquor (NH 4 Cl 190.6g / l, Na 2 SO 4 9.94g / l, NaCl 220g / l) and 6.34m 3 Reaction of deammonization mother liquor with lime and refining with lime and calcium chloride to remove magnesium and sulfate ions to obtain magnesium hydroxide, calcium sulfate precipitate and sulfur-removing brine, adding soda ash to remove sulfur-removing brine to obtain refined brine and calcium carbonate precipitate 276.34m obtained after refining 3 Refined brine (NaCl 288g / l, Na 2 SO 4 6.26g / l) and ammonia (NH 3 ), carbon dioxide (CO 2 ) as a raw material for metathesis reaction (reaction temperature 30°C) to separate and obtain 43 tons of solid sodium bicarbonate (NaHCO 3 ) and 276.34m 3 Contains ammonium chloride, sodium chloride and sodium sulfate (NaCl 138g / l, Na 2 SO 4 6.26g / l, NH 4 Cl 220g / l) and ammonium bicarbonat...

Embodiment 3

[0028] Embodiment 3: take 100m 3 Lake salt brine (NaCl 300g / l, Na 2 SO 4 15g / l, MgSO4 0.30g / l, CaSO 4 2.0g / l) and 170m 3 Ammonium making mother liquor (NH 4 Cl 190.6g / l, Na 2 SO 4 9.94g / l, NaCl 220g / l) and 6.34m 3 Reaction of deammonization mother liquor with lime and refining with lime and calcium chloride to remove magnesium and sulfate ions to obtain magnesium hydroxide, calcium sulfate precipitate and sulfur-removing brine, adding soda ash to remove sulfur-removing brine to obtain refined brine and calcium carbonate precipitate 276.34m obtained after refining 3 Refined brine (NaCl 288g / l, Na 2 SO 4 6.26g / l) and ammonia (NH 3 ), carbon dioxide (CO 2 ) as a raw material for metathesis reaction (reaction temperature 30°C) to separate and obtain 43 tons of solid sodium bicarbonate (NaHCO 3 ) and 276.34m 3 Contains ammonium chloride, sodium chloride and sodium sulfate (NaCl 138g / l, Na 2 SO 4 6.26g / l, NH 4 Cl 220g / l) and ammonium bicarbonate (NH 4 HCO 3 ),...

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Abstract

The invention provides a heat-cycle ammonia combined-soda process of brine with well salt, mineral salt, sea salt and lake salt. The process comprises the following steps: taking brine with well salt, mineral salt, sea salt and lake salt as the raw material, enabling the brine to react with an ammonia production mother solution and one part of deamination mother solution and lime to refine and obtain magnesium hydroxide, calcium sulfate and desulphuration brine, adding soda into the desulphuration brine to obtain refined brine and calcium carbonate, enabling the refined brine to react with ammonia and carbon dioxide to obtain sodium bicarbonate and a sodium hydrogen mother solution; removing ammonium bicarbonate and ammonium carbonate of the sodium hydrogen mother solution to obtain ammonia, carbon dioxide and the deamination mother solution; evaporating and separating one part of the deamination mother solution to obtain solid ammonia chloride and the ammonia production mother solution, combining the other part of the deamination mother solution into the raw material, enabling ammonia chloride to react with one part of lime to obtain ammonia and calcium chloride, and enabling calcium chloride to react with sodium sulfate to generate calcium sulfate; enabling magnesium sulfate and magnesium chloride in the raw material to react with the other part of lime to generate calcium sulfate and magnesium hydroxide precipitate; adding soda into the desulphuration brine after separating calcium sulfate and magnesium hydroxide precipitate to obtain refined brine and calcium carbonate precipitate; and enabling the refined brine to be continuously subjected to the above double decomposition reaction.

Description

technical field [0001] The invention belongs to the technical field of inorganic chemical industry, in particular to a process for producing soda ash, ammonium chloride and calcium chloride by directly using well, mine, sea and lake salt brine as raw material and adopting thermal circulation method. Background technique [0002] Known production soda ash process has the Lublan method, ammonia soda method and cold method combined soda ash method, wherein: 1) soda ash produced by the Lublin method: The Lublan method has poor product quality, high production cost, large labor consumption and production Process is all carried out between solid phases, is difficult to the shortcoming such as continuous operation; 2) Solvay process alkali: Solvay process (ammonia soda process) raw material sodium chloride utilization rate is low (the utilization rate of sodium is about 75%, the utilization of chlorine rate of 0%), distillation waste liquid (contains a large amount of calcium chlor...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C01D7/18C01F11/28C01C1/16
CPCC01C1/164C01D7/18C01F11/28
Inventor 彭赛军彭志成
Owner CHINA LIGHT IND INT ENG CO LTD