CN216191116U - System for magnesium process desulfurization liquid magnesium sulfate coproduction high-purity magnesite and ammonium sulfate - Google Patents
System for magnesium process desulfurization liquid magnesium sulfate coproduction high-purity magnesite and ammonium sulfate Download PDFInfo
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Abstract
A system for co-producing high-purity magnesite and ammonium sulfate from magnesium desulfurization liquid magnesium sulfate belongs to the technical field of industrial wastewater treatment. The method has the advantages that the magnesium in the magnesium sulfate of the desulfurization liquid is partially converted into high-purity magnesia, the rest is converted into light magnesium carbonate, sulfur in the magnesium sulfate is completely converted into chemical products with high quality, high benefit and large market demand of ammonium sulfate, the complex process problem in the prior art is reduced, the operation difficulty is reduced, the potential soluble solid waste hidden danger of magnesium sulfate heptahydrate is eliminated while the formation of the desulfurization gypsum solid waste is avoided, the ultralow emission target is comprehensively realized, the waste liquid treatment mode which changes waste into valuable and is convenient for industrial development is provided, the method is particularly suitable for coal-fired power plants, and the method has practical guiding effect and long-term development significance in the traditional limestone-gypsum desulfurization process switching magnesium desulfurization.
Description
Technical Field
The utility model belongs to the technical field of industrial wastewater treatment, and particularly relates to a system for co-producing high-purity magnesite and ammonium sulfate from desulfurization liquid magnesium sulfate by a flue gas magnesium method.
Background
The magnesium desulfurization of flue gas is widely applied to various industrial fields, especially plays an important role in flue gas treatment in the industries such as thermoelectricity and the like, and the desulfurization effect reaches the technical level of ultralow emission.
Magnesium desulfurization, the main component of the final desulfurization product is magnesium sulfate aqueous solution, and the existing treatment method is to obtain magnesium sulfate heptahydrate by evaporation, cooling and crystallization. The magnesium sulfate is affected by denitration and desulfurization due to the complex components of the flue gas, the desulfurization solution contains VOC, soluble ammonium salt, soluble sodium salt and other trace components besides the main component magnesium sulfate, and the impurities are mixed into the crystallization product magnesium sulfate heptahydrate, so that the problems of product difference, low main component content and the like are caused, and the magnesium sulfate can only be used as a cheap agricultural product. The method can also realize balanced sale for enterprises with producing areas close to using areas, but for the enterprises in remote areas, the enterprises can not realize balanced treatment on site, and only can store the soluble solid wastes which become extremely harmful.
Obviously, only the desulfurization product magnesium sulfate waste liquid is converted into a product with high added value and wide market demand, the magnesium desulfurization can be better developed, and the progress of switching the calcium desulfurization with limestone-gypsum to the magnesium desulfurization is guided.
29.01.1, CN 112279277A discloses the applicant's "a system and method for high-end resource utilization of flue gas desulfurization by magnesium method", patent application No. 202011341636.4.
The utility model aims to provide a system and a method for flue gas magnesium desulphurization resource output, which realize zero discharge of waste residue and wastewater by converting all harmful substance elements in a magnesium desulphurization system into chemical products with high quality, high benefit and large market demand.
The method is based on flue gas magnesium desulphurization, takes the high value-added resource transfer of the desulphurization solution magnesium sulfate as a main line, and firstly converts a part of magnesium sulfate to obtain magnesium sulfate series products by adopting an evaporative crystallization mode; secondly, potassium sulfate is obtained through the reaction of introduced potassium chloride and sulfate radicals in the desulfurization solution magnesium sulfate; thirdly, the intervention sodium carbonate reacts with the residual magnesium ions existing in the form of magnesium chloride to precipitate magnesium carbonate to obtain high-end magnesium salt products of fused magnesite; fourthly, obtaining the byproduct industrial salt by evaporating and crystallizing chloride with sodium chloride as a main component; fifthly, evaporating and crystallizing ammonium salt with ammonium sulfate as a main component to obtain the ammonium-based fertilizer.
The method well achieves the aim of resource conversion of the desulfurization solution, obtains products with high added value and commercial value and market demand, and also practically realizes the discharge of waste residue, waste water and zero and simultaneously thoroughly solves the problem of solid waste disposal, but has the defects of beauty, and mainly reflects the problems of overlong process chain, increased control difficulty and higher implementation and popularization technical requirements.
Therefore, it is necessary to develop a better and simpler way for recycling the desulfurized liquid magnesium sulfate waste liquid based on the technical advantages, and to make the flue gas magnesium desulfurization resource efficient utilization system and method better and more advanced.
Disclosure of Invention
The utility model aims to provide a system for co-producing high-purity magnesite and ammonium sulfate by using magnesium-method desulfurization liquid magnesium sulfate, so that magnesium in the desulfurization liquid magnesium sulfate is partially converted into high-purity magnesite, the rest part of the desulfurization liquid magnesium sulfate is converted into light magnesium carbonate, sulfur in the desulfurization liquid magnesium sulfate is completely converted into an ammonium sulfate product, all substance elements in the desulfurization liquid are converted into high-quality chemical products with high benefit and large market demands, and the aim of zero discharge of waste residues and waste water is fulfilled.
In order to achieve the aim, the utility model provides a system for coproducing high-purity magnesite and ammonium sulfate from magnesium process desulfurization liquid magnesium sulfate, which is formed by sequentially associating a plurality of chemical units according to a chemical reaction process, and is characterized in that:
p1: the high-purity magnesia MgO product preparation subsystem sequentially consists of a purification and impurity removal unit, a concentration adjustment ammonia precipitation unit, a filtration and washing 1 unit, a drying unit and a high-temperature electric melting unit;
p2: sequentially precipitating MgCO3The unit, the filtration washing 2 unit, the heat conversion unit, the filtration unit and the drying and crushing unit form light magnesium carbonate 4MgCO3·Mg(OH)2·4H2O product preparation subsystem;
p3: sequentially comprises a multi-effect evaporation concentration unit and a crystallization separation unit to form agricultural ammonium sulfate (NH)4)2SO4A product preparation subsystem;
p4: the purifying and impurity removing unit consists of a desulfurizing liquid MgSO4Feed inlet and cleaned MgSO4A solution outlet which is communicated with the inlet of the concentration adjustment ammonia precipitation unit; the concentration adjustment ammonia precipitation unit is also provided with a solution condensed water inlet, a washing liquid 1 inlet, an ammonia water inlet and a slurry outlet communicated with the slurry inlet of the filtration washing 1 unit; the unit for filtering and washing 1 is also provided with a pure water inlet, a filtrate 1 outlet, a washing liquid 1 outlet and a magnesium hydroxide filter material outlet, wherein the filtrate 1 outlet and the precipitated MgCO are connected3The inlet of the unit filtrate 1 is communicated with the outlet of the washing liquid 1, and the outlet of the washing liquid 1 is respectively connected with the inlet of the washing liquid 1 of the concentration adjustment ammonia precipitation unit 2 and the precipitated MgCO3The inlet of the washing liquid 1 of the unit 6 is communicated, and the outlet of the magnesium hydroxide filter material is communicated with the inlet of the drying unit; the drying unit is provided with a pure water (steam condensate) outlet and a dry material outlet besides a steam inlet, the dry material outlet is communicated with a feed inlet of the high-temperature electric melting unit, the high-temperature electric melting unit is also provided with a high-purity magnesia MgO product outlet for precipitating MgCO3The unit is provided with ammonium bicarbonate NH4HCO3A feed inlet, an ammonia water inlet, a filtrate 1, a washing liquid 2 inlet and a slurry outlet, wherein the filtrate 1 inlet is communicated with the filtrate 1 outlet of the filtration washing 1 unit, the washing liquid 1 inlet is communicated with the washing liquid 1 outlet of the filtration washing 1 unit, and the washing liquid 2 inlet is communicated with the filtration washing 2 unitThe discharge port of the washing liquid 2 is communicated, the slurry discharge port of the washing liquid 2 is communicated with the feed port of the filtration and washing 2 unit, the filtration and washing 2 unit is also provided with a solution condensate water injection port, a washing liquid 2 discharge port, a filtrate 2 discharge port and a filter material discharge port, and the washing liquid 2 discharge port is communicated with the precipitated MgCO3The feed inlet of the unit washing liquid 2 is communicated, the discharge outlet of the filtrate 2 is communicated with the feed inlet of the multi-effect evaporation concentration unit, and the discharge outlet of the filter material is communicated with the feed inlet of the heat conversion unit; the heat conversion unit is also provided with a pure water filling port, a steam inlet, a filtrate 3 inlet, a condensed water outlet and a slurry outlet, wherein the slurry outlet is communicated with the slurry feeding port of the filtering unit, and the filtrate 3 inlet is communicated with the filtrate 3 outlet of the filtering unit; the discharge port of the filtering unit is communicated with the feed port of the drying and crushing unit, and the drying and crushing unit is also provided with a steam inlet, a pure water (steam condensate) discharge port and light magnesium carbonate 4MgCO3·Mg(OH)2·4H2O, product outlet; the filtrate 2 discharge port of the filtering and washing unit 2 is communicated with the feed port of the multi-effect evaporation and concentration unit, and the multi-effect evaporation and concentration unit is also provided with a steam inlet, a pure water (steam condensate) discharge port, a solution condensate discharge port, a concentrated solution discharge port communicated with the feed port of the crystallization separation unit and a mother solution return port communicated with the mother solution discharge port of the crystallization separation unit; the crystallization separation unit is also provided with agricultural ammonium sulfate (NH)4)2SO4A product outlet; the steam condensed water (pure water) outlet of the drying unit, the drying and crushing unit and the multi-effect evaporation and concentration unit are communicated with the pure water inlet of the filtration and washing unit 1 and the pure water inlet of the heat conversion unit, and the solution condensed water (solution evaporation condensed water) outlet of the multi-effect evaporation and concentration unit is respectively communicated with the solution condensed water inlet of the concentration adjustment ammonia precipitation unit and the solution condensed water inlet of the filtration and washing unit 2.
The system for co-producing high-purity magnesite and ammonium sulfate from magnesium process desulfurization liquid magnesium sulfate has the advantages that the use industry generally has the advantages of waste heat air, waste heat flue gas and the like, the waste heat can be utilized, the waste heat is collectively called waste hot air, and the heat pollution can be reduced, and the system materials can also be heated and pre-evaporated by utilizing the waste heat. In a similar way, the drying unit and the drying and crushing unit of the system can generate drying hot air with a certain temperature, and can also be used for heating and pre-evaporating system materials, particularly the drying hot air of the drying unit can contain trace magnesium hydroxide dust, the drying and crushing unit can also contain trace light magnesium carbonate dust, and the dust has a desulfurization effect, can be used for further desulfurization of the system, and achieves a gas washing effect through gas-liquid exchange, so that the system is more perfect.
Thus, the preferred solutions that result are:
the drying unit of the P1 subsystem further comprises a drying hot air outlet; the drying and crushing unit of the P2 subsystem further comprises a drying hot air outlet; the P3 subsystem further comprises a washing concentration desulfurization dust removal unit and a filtering purification unit, wherein the washing concentration desulfurization dust removal unit is provided with a waste hot air inlet, a dry hot air inlet, a purified flue gas exhaust port, a filtrate 2 feeding port and a discharging port, the dry hot air inlet is respectively communicated with the dry hot air outlets of the drying unit and the drying and crushing unit through pipelines, the filtrate 2 feeding port is communicated with the filtrate 2 discharging port of the filtering and washing 2 unit, the discharging port is communicated with the feeding port of the filtering purification unit, and the filtering purification unit further comprises a discharging port communicated with the feeding port of the multi-effect evaporation concentration unit.
In addition, the optimized scheme has the condition of inconvenient use of the waste hot air, which does not hinder the operation of the system of the utility model, and the air inlet of the waste hot air is closed or cancelled, namely the characteristic arrangement of the air inlet of the waste hot air is cancelled in the scrubbing, concentrating, desulfurizing and dedusting unit of the P3 subsystem.
The utility model relates to a system for co-producing high-purity magnesite clinker and ammonium sulfate from magnesium desulfurization liquid, wherein a purification and impurity removal unit in a P1 subsystem is not labeled with aerated magnesium sulfite and COD influence elimination, and the system is a conventional operation considering that the flue gas desulfurization unit performs the operation by utilizing waste heat air (waste hot air) and performs primary slag stone screening.
The utility model relates to a system for coproducing high-purity magnesite and ammonium sulfate by using magnesium desulfurization liquid magnesium sulfate, wherein a purification and impurity removal unit in a P1 subsystem does not mark what impurities are filtered and removed, because the impurities are mostly solid powder such as raw stone slag materials with small particles, and the like, the impurities are nontoxic and tasteless, the content and the quantity of the impurities are very little compared with the treatment capacity of the system, and the impurities can be periodically accumulated for landfill or returned to a fly ash utilization system for utilization. Similarly, the situation of the fly ash filtered by the filtering and impurity removing unit of the P3 subsystem is the same as that of the fly ash filtered by the filtering and impurity removing unit, and the fly ash can be treated as above.
The utility model relates to a system for coproducing high-purity magnesite and ammonium sulfate from magnesium-process desulfurization liquid magnesium sulfate, wherein no circulating washing gas is marked in a washing gas concentration desulfurization dust removal unit in a P3 subsystem, and the circulating washing gas is not excluded in the utility model, which belongs to the technical common practice, and the required cycle number can be comprehensively determined according to the concentration of the solution and the suitable evaporation efficiency.
The ammonia water of the utility model is generally concentrated ammonia water.
The ammonium bicarbonate of the present invention broadly refers to agricultural ammonium bicarbonate.
The heat source adopted by the evaporation is steam, and the steam can be replaced by fuel gas, electric energy and the like.
The utility model relates to a system for coproducing high-purity magnesite and ammonium sulfate from magnesium process desulfurization liquid magnesium sulfate, wherein each unit of the system can be decomposed or combined as necessary, and the decomposition and combination follow the common chemical reaction principle and do not form the creative breakthrough of the utility model.
The utility model relates to a system for coproducing high-purity magnesite and ammonium sulfate by using magnesium-method desulfurized liquid magnesium sulfate, which takes magnesium-method desulfurized liquid magnesium sulfate as a raw material, converts the desulfurized liquid magnesium sulfate as a resource to a main line from a product with a high added value, adopts steam condensate water to replace pure water to wash a magnesium hydroxide filter material and adjust the heat conversion solid content, uses solution condensate water obtained by multi-effect evaporation of the ammonium sulfate solution to wash the magnesium carbonate filter material, uses the purified magnesium sulfate solution and intervened ammonia to perform an ammonia precipitation reaction to obtain a magnesium hydroxide intermediate product and an ammonium sulfate transition solution, and uses electric energy to perform high-temperature electric melting on magnesium hydroxide washed by the pure water (steam condensate water) to obtain high-purity magnesite in a high added value and large market; the magnesium sulfate solution which is not completely converted into magnesium hydroxide is continuously subjected to precipitation reaction and thermal transformation reaction with intervening ammonium bicarbonate and ammonia water to obtain a light magnesium carbonate intermediate product and an ammonium sulfate transition solution, and a filtered light magnesium carbonate (also called magnesium carbonate) filter material is subjected to steam drying and crushing to obtain a light magnesium carbonate product; after the ammonium sulfate transition solution is subjected to gas washing, concentration, desulfurization and dust removal, the ammonium sulfate solution is heated and even concentrated; the purified ammonium sulfate solution is subjected to multi-effect evaporation concentration and cooling crystallization separation to obtain an agricultural ammonium sulfate product; the steam condensate water (also called pure water) of the heat conversion and multi-effect evaporation concentration unit returns to the filtering and washing unit of the system to wash filter cakes (filter materials), and the mother liquor of the crystallization separation unit returns to the multi-effect evaporation concentration unit to be evaporated repeatedly, so that a closed system and a process system are formed.
Therefore, magnesium (magnesium ions) in the magnesium sulfate waste liquid entering the system are respectively converted into magnesium hydroxide and magnesium carbonate intermediate products (filter materials) with higher purity and capable of being washed by pure water, and the magnesium hydroxide and magnesium carbonate intermediate products can be deeply converted into high-purity magnesite and light magnesium carbonate products with extremely high purity, excellent performance and extremely low cost through drying and high-temperature calcination by electric energy; the sulfur (sulfate ion) in the magnesium sulfate, the intervening ammonia water and the ammonium ion in the ammonium bicarbonate generate ammonium sulfate, and finally the ammonium sulfate product is obtained through concentration and crystallization; the desulfurization solution also contains trace components such as partially soluble nitrates (sodium, iron), chlorides and the like, and the trace components enter the ammonium sulfate product along with the crystallization of the ammonium sulfate, so the comprehensive content of the trace components is very low, and the product quality requirement of the agricultural ammonium sulfate is not influenced. Therefore, the desulfurization liquid magnesium sulfate waste liquid is completely extracted by orderly recycling waste wastes, the emission of waste residues, waste water and zero is realized fundamentally, on the basis of reasonably utilizing the advantages of waste hot air and dry hot air, sulfate ions in the desulfurization liquid are converted into agricultural ammonium sulfate fertilizer required by large market, and the confusion and interference of the formation of mixed gypsum byproducts to the desulfurization industry are successfully avoided.
Compared with the prior art, the system for co-producing high-purity magnesite and ammonium sulfate by using magnesium desulfurization liquid magnesium sulfate has the beneficial effects that:
the utility model relates to a system for coproducing high-purity magnesite and ammonium sulfate from magnesium-method desulfurization liquid magnesium sulfate, which utilizes a means of precipitating high-purity substances by an ionic reaction between solutions to convert magnesium in the magnesium sulfate into high-purity magnesite and light magnesium carbonate products, convert sulfur in the magnesium sulfate into agricultural ammonium sulfate products, purify and remove impurities from the desulfurization liquid entering the system, and use pure water regenerated by the system as system water to ensure the product quality of the system, thereby obtaining products with large market demands, high added value quality and low production cost, simultaneously shortening the fussy problem of the prior art process and reducing the operation difficulty, avoiding the potential soluble solid waste hidden danger of magnesium sulfate heptahydrate while avoiding the formation of the solid waste of the desulfurization gypsum, realizing the ultra-low emission target, contributing to the waste and turning waste into wealth, facilitating the industrial development of waste liquid treatment mode, and being particularly suitable for use in coal-fired power plants, especially, the method has practical guiding function and long-term development significance for the traditional limestone-gypsum desulfurization process to switch the magnesium method desulfurization.
Drawings
The utility model is further described below with reference to the accompanying drawings and embodiments, it is obvious that the drawings in the following description are only some embodiments of the utility model, and that other drawings can be obtained by those skilled in the art without inventive effort.
FIG. 1 is a schematic view of a basic scheme of a system for co-producing high-purity magnesite clinker and ammonium sulfate from magnesium process desulfurization liquid magnesium sulfate provided by the utility model.
FIG. 2 is a schematic view of an optimized scheme of the system for co-producing high-purity magnesite clinker and ammonium sulfate from magnesium process desulfurization liquid magnesium sulfate provided by the utility model.
FIG. 3 is a schematic diagram showing the characteristic identification of the basic scheme of the system for co-producing high-purity magnesite clinker and ammonium sulfate by using magnesium desulfurization liquid magnesium sulfate.
FIG. 4 is a schematic diagram of the characteristic identification of the optimization scheme of the system for co-producing high-purity magnesite clinker and ammonium sulfate by using magnesium desulfurization liquid magnesium sulfate.
As can be seen from the figures 1 and 2, the system of the utility model is clear at a glance, and the content of the utility model can be intuitively and clearly explained.
As can be seen from fig. 3 and 4, the system of the present invention has clear technical features, and can accurately explain the contents of the utility model and the contents of the claims.
In FIGS. 3 and 4
1-purifying and impurity removing unit, 2-concentration adjusting ammonia precipitation unit, 3-filtering and washing 1 unit,
4-drying unit, 5-high temperature electric melting unit, 6-precipitation MgCO3The unit cell is a unit cell, which is composed of a plurality of unit cells,
7-filtration washing 2 unit, 8-heat transformation unit, 9-filtration unit,
10-drying and crushing unit, 11-washing, concentrating, desulfurizing and dedusting unit, 12-filtering and purifying unit,
13-multiple-effect evaporation concentration unit, 14-crystallization separation unit.
Detailed Description
Example 1: as can be seen from FIG. 3, the utility model provides a basic implementation mode of a system for co-producing high-purity magnesite and ammonium sulfate by magnesium desulphurization liquid magnesium sulfate, which is formed by sequentially associating a plurality of chemical units according to a chemical reaction process, and is characterized in that:
p1: the high-purity magnesia MgO product preparation subsystem sequentially consists of a purification and impurity removal unit 1, a concentration adjustment ammonia precipitation unit 2, a filtering and washing unit 1, a drying unit 4 and a high-temperature electric melting unit 5;
p2: sequentially precipitating MgCO3The unit 6, the filtering and washing 2 unit 7, the heat conversion unit 8, the filtering unit 9 and the drying and crushing unit 10 form light magnesium carbonate 4MgCO3·Mg(OH)2·4H2O product preparation subsystem;
p3: sequentially comprises a multi-effect evaporation concentration unit 13 and a crystallization separation unit 14 to form agricultural ammonium sulfate (NH)4)2SO4A product preparation subsystem;
p4: the purification and impurity removal unit 1 is composed of desulfurization solution MgSO4Feed inlet and cleaned MgSO4A solution outlet which is communicated with the inlet of the concentration adjustment ammonia precipitation unit 2; the concentration adjustment ammonia precipitation unit 2 is also provided with a solution condensed water inlet, a washing liquid 1 inlet, an ammonia water inlet and a slurry outlet communicated with the slurry inlet of the filtration washing unit 1 unit 3(ii) a The unit 3 of the filtering and washing 1 is also provided with a pure water inlet, a filtrate 1 outlet, a washing liquid 1 outlet and a magnesium hydroxide filter material outlet, wherein the filtrate 1 outlet and the precipitated MgCO are arranged3The inlet of the unit 6 filtrate 1 is communicated with the outlet of the washing liquid 1, and the outlet of the washing liquid 1 is respectively connected with the inlet of the washing liquid 1 of the concentration adjustment ammonia precipitation unit 2 and the precipitated MgCO3The washing liquid 1 feeding port of the unit 6 is communicated with the magnesium hydroxide filtering material discharging port of the unit is communicated with the drying unit 4 feeding port; the drying unit 4 is provided with a pure water (steam condensate) outlet and a dry material outlet besides a steam inlet, the dry material outlet is communicated with a feed inlet of the high-temperature electric melting unit 5, the high-temperature electric melting unit 5 is also provided with a high-purity magnesia MgO product outlet, and MgCO is precipitated3The unit 6 is provided with ammonium bicarbonate NH4HCO3A feed inlet, an ammonia water filling port, a filtrate 1, a washing liquid 2 feed inlet and a slurry discharge port, wherein the filtrate 1 feed inlet is communicated with a filtrate 1 discharge port of a filtration washing 1 unit 3, the washing liquid 1 feed inlet is communicated with a washing liquid 1 discharge port of the filtration washing 1 unit 3, the washing liquid 2 feed inlet is communicated with a washing liquid 2 discharge port of a filtration washing 2 unit 7, the slurry discharge port is communicated with a feed inlet of the filtration washing 2 unit 7, the filtration washing 2 unit 7 is also provided with a solution condensed water filling port, a washing liquid 2 discharge port, a filtrate 2 discharge port and a filter material discharge port, and the washing liquid 2 discharge port is communicated with precipitated MgCO3The unit 6 is communicated with the feeding hole of the washing liquid 2, the discharging hole of the filtrate 2 is communicated with the feeding hole of the multi-effect evaporation concentration unit 13, and the discharging hole of the filter material is communicated with the feeding hole of the heat conversion unit 8; the heat conversion unit 8 is also provided with a pure water filling opening, a steam inlet, a filtrate 3 inlet, a condensed water discharging opening and a slurry discharging opening, wherein the slurry discharging opening is communicated with a slurry feeding opening of the filtering unit 9, and the filtrate 3 inlet is communicated with a filtrate 3 discharging opening of the filtering unit 9; the discharge port of the filtering unit 9 is communicated with the feed port of the drying and crushing unit 10, and the drying and crushing unit 10 is also provided with a steam inlet, a pure water (steam condensate) discharge port and light magnesium carbonate 4MgCO3·Mg(OH)2·4H2O, product outlet; the filtrate 2 discharge port of the filtering and washing unit 27 is communicated with the feed port of the multi-effect evaporation concentration unit 13, and the multi-effect evaporation concentration unit 13 is also provided with a steam inlet, a pure water (steam condensate) discharge port and a solution condensate discharge portAn outlet, a concentrated solution outlet communicated with the feeding inlet of the crystallization separation unit 14 and a mother solution return outlet communicated with the mother solution outlet of the crystallization separation unit 14; the crystallization separation unit 14 is also provided with agricultural ammonium sulfate (NH)4)2SO4A product outlet; the steam condensed water (pure water) discharge ports of the drying unit 4, the drying and crushing unit 10 and the multi-effect evaporation and concentration unit 13 are communicated with pure water injection ports of the filtration and washing 1 unit 3 and the heat transfer unit 8, and the solution condensed water (solution evaporation condensed water) discharge port of the multi-effect evaporation and concentration unit 13 is respectively communicated with a solution condensed water inlet port of the concentration adjustment ammonia precipitation unit 2 and a solution condensed water injection port of the filtration and washing 2 unit 7.
Example 2: as can be seen from FIG. 4, the utility model provides an optimized implementation mode of a system for co-producing high-purity magnesite clinker and ammonium sulfate by magnesium desulphurization liquid magnesium sulfate, which is formed by sequentially associating a plurality of chemical units according to a chemical reaction process, and is characterized in that:
p1: the high-purity magnesia MgO product preparation subsystem sequentially consists of a purification and impurity removal unit 1, a concentration adjustment ammonia precipitation unit 2, a filtering and washing unit 1, a drying unit 4 and a high-temperature electric melting unit 5;
p2: sequentially precipitating MgCO3The unit 6, the filtering and washing 2 unit 7, the heat conversion unit 8, the filtering unit 9 and the drying and crushing unit 10 form light magnesium carbonate 4MgCO3·Mg(OH)2·4H2O product preparation subsystem;
p3: sequentially comprises a scrubbing, concentrating, desulfurizing and dedusting unit 11, a filtering and purifying unit 12, a multi-effect evaporation and concentration unit 13 and a crystallization and separation unit 14 to form agricultural ammonium sulfate (NH)4)2SO4A product preparation subsystem;
p4: the purification and impurity removal unit 1 is composed of desulfurization solution MgSO4Feed inlet and cleaned MgSO4A solution outlet which is communicated with the inlet of the concentration adjustment ammonia precipitation unit 2; the concentration adjustment ammonia precipitation unit 2 is also provided with a solution condensed water inlet, a washing liquid 1 inlet, an ammonia water inlet and a slurry outlet communicated with the slurry inlet of the unit 3 of the filtration washing 1; the unit 3 for filtration and washing 1 is further provided with a pure water inlet, a filtrate 1 outlet, and a washing liquid1 discharge port and magnesium hydroxide filter material discharge port, and filtrate 1 discharge port and precipitated MgCO3The feed inlet of the filtrate 1 of the unit 6 is communicated with the discharge outlet of the washing liquid 1 of the unit 6 and the precipitated MgCO3The inlet of the washing liquid 1 of the unit 6 is communicated with the outlet of the washing liquid 1, and the outlet of the washing liquid 1 is respectively connected with the inlet of the washing liquid 1 of the concentration adjustment ammonia precipitation unit 2 and the precipitated MgCO3The washing liquid 1 feeding port of the unit 6 is communicated with the magnesium hydroxide filtering material discharging port of the unit is communicated with the drying unit 4 feeding port; the drying unit 4 is provided with a steam inlet, a pure water (steam condensate) outlet and a dry material outlet, and is also provided with a dry hot air outlet which is communicated with a dry hot air inlet of the scrubbing, concentrating, desulfurizing and dedusting unit 11 through a pipeline, the dry material outlet is communicated with a feed inlet of the high-temperature electric melting unit 5, and the high-temperature electric melting unit 5 is also provided with a high-purity magnesia MgO product outlet; precipitation of MgCO3The unit 6 is provided with ammonium bicarbonate NH4HCO3A feed inlet, an ammonia water filling port, a filtrate 1, a washing liquid 2 feed inlet and a slurry discharge port, wherein the filtrate 1 feed inlet is communicated with a filtrate 1 discharge port of a filtration washing 1 unit 3, the washing liquid 1 feed inlet is communicated with a washing liquid 1 discharge port of the filtration washing 1 unit 3, the washing liquid 2 feed inlet is communicated with a washing liquid 2 discharge port of a filtration washing 2 unit 7, the slurry discharge port is communicated with a feed inlet of the filtration washing 2 unit 7, the filtration washing 2 unit 7 is also provided with a solution condensed water filling port, a washing liquid 2 discharge port, a filtrate 2 discharge port and a filter material discharge port, and the washing liquid 2 discharge port is communicated with precipitated MgCO3The unit 6 is communicated with the feeding hole of the washing liquid 2, the discharging hole of the filtrate 2 is communicated with the feeding hole of the multi-effect evaporation concentration unit 13, and the discharging hole of the filter material is communicated with the feeding hole of the heat conversion unit 8; the heat conversion unit 8 is also provided with a pure water filling opening, a steam inlet, a filtrate 3 inlet, a condensed water discharging opening and a slurry discharging opening, wherein the slurry discharging opening is communicated with a slurry feeding opening of the filtering unit 9, and the filtrate 3 inlet is communicated with a filtrate 3 discharging opening of the filtering unit 9; the discharge port of the filtering unit 9 is communicated with the feed port of the drying and crushing unit 10, and the drying and crushing unit 10 is also provided with a steam inlet, a pure water (steam condensate) discharge port and light magnesium carbonate 4MgCO3·Mg(OH)2·4H2O, product outlet; the discharge port of the filtrate 2 and the concentration of the washing gas in the filtration and washing 2 unit 7The filtrate 2 feed inlet of the shrinkage, desulfurization and dust removal unit 11 is communicated, the scrubbing, concentration, desulfurization and dust removal unit 11 is also provided with a waste hot air inlet, a dry hot air inlet, a purified flue gas exhaust port and a discharge port, the dry hot air inlet is respectively communicated with the dry hot air outlets of the drying unit 4 and the drying and crushing unit 10 through pipelines, the discharge port is communicated with the feed inlet of the filtering and purifying unit 12, and the filtering and purifying unit 12 further comprises a discharge port communicated with the feed inlet of the multi-effect evaporation and concentration unit 13; the multi-effect evaporation concentration unit 13 is also provided with a steam inlet, a pure water (steam condensate) outlet, a solution condensate outlet, a concentrated solution outlet communicated with the feed inlet of the crystallization separation unit 14 and a mother solution return inlet communicated with the mother solution outlet of the crystallization separation unit 14; the crystallization separation unit 14 is also provided with agricultural ammonium sulfate (NH)4)2SO4A product outlet; the steam condensed water (pure water) discharge ports of the drying unit 4, the drying and crushing unit 10 and the multi-effect evaporation and concentration unit 13 are communicated with pure water injection ports of the filtration and washing 1 unit 3 and the heat transfer unit 8, and the solution condensed water (solution evaporation condensed water) discharge port of the multi-effect evaporation and concentration unit 13 is respectively communicated with a solution condensed water inlet port of the concentration adjustment ammonia precipitation unit 2 and a solution condensed water injection port of the filtration and washing 2 unit 7.
Claims (4)
1. The utility model provides a system for magnesium process desulfurization liquid magnesium sulfate coproduction high-purity magnesite and ammonium sulfate comprises according to chemical industry reaction process relevance in proper order by a plurality of chemical industry units, its characterized in that:
p1: the high-purity magnesia MgO product preparation subsystem consists of a purification and impurity removal unit (1), a concentration adjustment ammonia precipitation unit (2), a filtration and washing unit (3), a drying unit (4) and a high-temperature electric melting unit (5) in sequence;
p2: sequentially precipitating MgCO3The light magnesium carbonate 4MgCO is formed by a unit (6), a filtering and washing 2 unit (7), a heat conversion unit (8), a filtering unit (9) and a drying and crushing unit (10)3·Mg(OH)2·4H2O product preparation subsystem;
p3: sequentially comprises a multi-effect evaporation concentration unit (13) and a crystallization separation unit (14) to form agricultural ammonium sulfate (NH)4)2SO4A product preparation subsystem;
p4: the purification and impurity removal unit (1) is composed of a desulfurization solution MgSO4Feed inlet and cleaned MgSO4A solution discharge port which is communicated with a feed port of the concentration adjustment ammonia precipitation unit (2); the concentration adjustment ammonia precipitation unit (2) is also provided with a solution condensed water inlet, a washing liquid 1 inlet, an ammonia water inlet and a slurry outlet communicated with the slurry inlet of the filtering and washing unit 1 (3); the unit (3) of the filtering and washing 1 is also provided with a pure water inlet, a filtrate 1 outlet, a washing liquid 1 outlet and a magnesium hydroxide filter material outlet, wherein the filtrate 1 outlet and the precipitated MgCO are arranged3The inlet of the filtrate 1 of the unit (6) is communicated with the outlet of the washing liquid 1 of the unit (6), and the outlet of the washing liquid 1 is respectively communicated with the inlet of the washing liquid 1 of the concentration adjustment ammonia precipitation unit (2) and the precipitated MgCO3The feed inlet of the washing liquid 1 of the unit (6) is communicated, and the discharge outlet of the magnesium hydroxide filter material is communicated with the feed inlet of the drying unit (4); the drying unit (4) is provided with a pure water outlet and a dry material outlet besides a steam inlet, the dry material outlet is communicated with a feed inlet of the high-temperature electric melting unit (5), the high-temperature electric melting unit (5) is also provided with a high-purity magnesia MgO product outlet for precipitating MgCO3The unit (6) is provided with ammonium bicarbonate NH4HCO3A feed inlet, an ammonia water filling port, a filtrate 1, a washing liquid 2 feed inlet and a slurry discharge port, wherein the filtrate 1 feed inlet is communicated with the filtrate 1 discharge port of the filtration washing 1 unit (3), the washing liquid 1 feed inlet is communicated with the washing liquid 1 discharge port of the filtration washing 1 unit (3), the washing liquid 2 feed inlet is communicated with the washing liquid 2 discharge port of the filtration washing 2 unit (7), the slurry discharge port is communicated with the filtration washing 2 unit (7), the filtration washing 2 unit (7) is also provided with a solution condensate water filling port, a washing liquid 2 discharge port, a filtrate 2 discharge port and a filter material discharge port, and the washing liquid 2 discharge port is communicated with precipitated MgCO3The feeding hole of the washing liquid 2 of the unit (6) is communicated, the discharging hole of the filtrate 2 is communicated with the feeding hole of the multi-effect evaporation concentration unit (13), and the discharging hole of the filter material is communicated with the feeding hole of the heat conversion unit (8); the heat conversion unit (8) is also provided with a pure water inlet, a steam inlet, a filtrate 3 inlet, a condensed water outlet and a slurry outlet, the slurry outlet is communicated with the slurry inlet of the filtering unit (9), the filtrate 3 inlet is communicated with the filtering unit (9)The discharge ports of the filtrate 3 are communicated; the discharge hole of the filtering unit (9) is communicated with the feed hole of the drying and crushing unit (10), and the drying and crushing unit (10) is also provided with a steam inlet, a pure water discharge hole and light magnesium carbonate 4MgCO3·Mg(OH)2·4H2O, product outlet; a discharge port of the filtrate 2 of the unit (7) for filtering and washing 2 is communicated with a feed port of the multi-effect evaporation and concentration unit (13), and the multi-effect evaporation and concentration unit (13) is also provided with a steam inlet, a pure water discharge port, a solution condensed water discharge port, a concentrated solution discharge port communicated with the feed port of the crystallization separation unit (14) and a mother solution return port communicated with a mother solution discharge port of the crystallization separation unit (14); the crystallization separation unit (14) is also provided with agricultural ammonium sulfate (NH)4)2SO4A product outlet; the steam condensed water discharge ports of the drying unit (4), the drying and crushing unit (10) and the multi-effect evaporation and concentration unit (13) are communicated with pure water injection ports of the filtration and washing 1 unit (3) and the heat conversion unit (8), and the solution condensed water discharge port of the multi-effect evaporation and concentration unit (13) is respectively communicated with a solution condensed water inlet port of the concentration adjustment ammonia precipitation unit (2) and a solution condensed water injection port of the filtration and washing 2 unit (7).
2. The system for co-producing high-purity magnesite clinker and ammonium sulfate by using magnesium process desulfurization liquid magnesium sulfate according to claim 1, which is characterized in that:
the drying unit (4) of the P1 subsystem further comprises a drying hot air outlet; the drying and crushing unit (10) of the P2 subsystem further comprises a drying hot air outlet; the P3 subsystem further comprises a washing concentration desulfurization dust removal unit (11) and a filtering purification unit (12), wherein the washing concentration desulfurization dust removal unit (11) is provided with a drying hot air inlet, a purified flue gas exhaust port, a filtrate 2 inlet and an outlet, the drying hot air inlet is respectively communicated with drying hot air outlets of the drying unit (4) and the drying crushing unit (10) through pipelines, the filtrate 2 inlet is communicated with a filtrate 2 outlet of the filtering and washing 2 unit (7), the outlet is communicated with a inlet of the filtering purification unit (12), and the filtering purification unit further comprises an outlet communicated with a inlet of the multi-effect evaporation concentration unit (13).
3. The system for co-producing high-purity magnesite clinker and ammonium sulfate by using magnesium process desulfurization liquid magnesium sulfate according to claim 2, which is characterized in that:
the scrubbing, concentrating, desulfurizing and dedusting unit (11) is also provided with a waste hot air inlet.
4. The system for co-producing high-purity magnesite clinker and ammonium sulfate by using magnesium process desulfurization liquid magnesium sulfate according to claim 3, which is characterized in that:
p1: the high-purity magnesia MgO product preparation subsystem consists of a purification and impurity removal unit (1), a concentration adjustment ammonia precipitation unit (2), a filtration and washing unit (3), a drying unit (4) and a high-temperature electric melting unit (5) in sequence;
p2: sequentially precipitating MgCO3The light magnesium carbonate 4MgCO is formed by a unit (6), a filtering and washing 2 unit (7), a heat conversion unit (8), a filtering unit (9) and a drying and crushing unit (10)3·Mg(OH)2·4H2O product preparation subsystem;
p3: the agricultural ammonium sulfate (NH) is composed of a scrubbing concentration desulfurization dust removal unit (11), a filtering purification unit (12), a multi-effect evaporation concentration unit (13) and a crystallization separation unit (14) in sequence4)2SO4A product preparation subsystem;
p4: the purification and impurity removal unit (1) is composed of a desulfurization solution MgSO4Feed inlet and cleaned MgSO4A solution discharge port which is communicated with a feed port of the concentration adjustment ammonia precipitation unit (2); the concentration adjustment ammonia precipitation unit (2) is also provided with a solution condensed water inlet, a washing liquid 1 inlet, an ammonia water inlet and a slurry outlet communicated with the slurry inlet of the filtering and washing unit 1 (3); the unit (3) of the filtering and washing 1 is also provided with a pure water inlet, a filtrate 1 outlet, a washing liquid 1 outlet and a magnesium hydroxide filter material outlet, wherein the filtrate 1 outlet and the precipitated MgCO are arranged3The feed inlet of the filtrate 1 of the unit (6) is communicated with the discharge outlet of the washing liquid 1 of the unit (6) and the precipitated MgCO3The inlet of the washing liquid 1 of the unit (6) is communicated with the outlet of the washing liquid 1, and the outlet of the washing liquid 1 is respectively communicated with the inlet of the washing liquid 1 of the concentration adjustment ammonia precipitation unit (2) and the precipitated MgCO3The washing liquid 1 inlet of the unit (6) is communicated with the magnesium hydroxide filter material outlet of the unit (6) and the drying unit (4) inletAre communicated with each other; the drying unit (4) is provided with a steam inlet, a pure water outlet and a dry material outlet, and is also provided with a dry hot air outlet which is communicated with a dry hot air inlet of the scrubbing, concentrating, desulfurizing and dedusting unit (11) through a pipeline, the dry material outlet is communicated with a feed inlet of the high-temperature electric melting unit (5), and the high-temperature electric melting unit (5) is also provided with a high-purity magnesia MgO product outlet; precipitation of MgCO3The unit (6) is provided with ammonium bicarbonate NH4HCO3A feed inlet, an ammonia water filling port, a filtrate 1, a washing liquid 2 feed inlet and a slurry discharge port, wherein the filtrate 1 feed inlet is communicated with the filtrate 1 discharge port of the filtration washing 1 unit (3), the washing liquid 1 feed inlet is communicated with the washing liquid 1 discharge port of the filtration washing 1 unit (3), the washing liquid 2 feed inlet is communicated with the washing liquid 2 discharge port of the filtration washing 2 unit (7), the slurry discharge port is communicated with the filtration washing 2 unit (7), the filtration washing 2 unit (7) is also provided with a solution condensate water filling port, a washing liquid 2 discharge port, a filtrate 2 discharge port and a filter material discharge port, and the washing liquid 2 discharge port is communicated with precipitated MgCO3The feeding hole of the washing liquid 2 of the unit (6) is communicated, the discharging hole of the filtrate 2 is communicated with the feeding hole of the multi-effect evaporation concentration unit (13), and the discharging hole of the filter material is communicated with the feeding hole of the heat conversion unit (8); the heat conversion unit (8) is also provided with a pure water filling opening, a steam inlet, a filtrate 3 inlet, a condensed water discharging opening and a slurry discharging opening, the slurry discharging opening is communicated with the slurry feeding opening of the filtering unit (9), and the filtrate 3 inlet is communicated with the filtrate 3 discharging opening of the filtering unit (9); the discharge hole of the filtering unit (9) is communicated with the feed hole of the drying and crushing unit (10), and the drying and crushing unit (10) is also provided with a steam inlet, a pure water discharge hole and light magnesium carbonate 4MgCO3·Mg(OH)2·4H2O, product outlet; a discharge port of a filtrate 2 of the filtering and washing 2 unit (7) is communicated with a feed port of a filtrate 2 of the scrubbing, concentrating, desulfurizing and dedusting unit (11), the scrubbing, concentrating, desulfurizing and dedusting unit (11) is also provided with a waste hot air inlet, a dry hot air inlet, a purified flue gas exhaust port and a discharge port, the dry hot air inlet is respectively communicated with a dry hot air outlet of the drying unit (4) and a dry hot air outlet of the drying and crushing unit (10) through pipelines, the discharge port is communicated with the feed port of the filtering and purifying unit (12), and the filtering and purifying unit(s) (a12) The device also comprises a discharge hole communicated with the feed inlet of the multi-effect evaporation concentration unit (13); the multi-effect evaporation concentration unit (13) is also provided with a steam inlet, a pure water outlet, a solution condensed water outlet, a concentrated solution outlet communicated with the feed inlet of the crystallization separation unit (14) and a mother solution return port communicated with the mother solution outlet of the crystallization separation unit (14); the crystallization separation unit (14) is also provided with agricultural ammonium sulfate (NH)4)2SO4A product outlet; the steam condensed water discharge ports of the drying unit (4), the drying and crushing unit (10) and the multi-effect evaporation and concentration unit (13) are communicated with pure water injection ports of the filtration and washing 1 unit (3) and the heat conversion unit (8), and the solution condensed water discharge port of the multi-effect evaporation and concentration unit (13) is respectively communicated with a solution condensed water inlet port of the concentration adjustment ammonia precipitation unit (2) and a solution condensed water injection port of the filtration and washing 2 unit (7).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122329872.0U CN216191116U (en) | 2021-09-20 | 2021-09-20 | System for magnesium process desulfurization liquid magnesium sulfate coproduction high-purity magnesite and ammonium sulfate |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122329872.0U CN216191116U (en) | 2021-09-20 | 2021-09-20 | System for magnesium process desulfurization liquid magnesium sulfate coproduction high-purity magnesite and ammonium sulfate |
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