CN216005237U - System for coproduction of magnesium hydroxide and magnesium ammonium sulfate from desulfurization liquid magnesium sulfate - Google Patents
System for coproduction of magnesium hydroxide and magnesium ammonium sulfate from desulfurization liquid magnesium sulfate Download PDFInfo
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- CN216005237U CN216005237U CN202121822166.3U CN202121822166U CN216005237U CN 216005237 U CN216005237 U CN 216005237U CN 202121822166 U CN202121822166 U CN 202121822166U CN 216005237 U CN216005237 U CN 216005237U
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Abstract
A system for co-producing magnesium ammonium sulfate by regenerating magnesium hydroxide from desulfurized liquid magnesium sulfate, belonging to the technical field of industrial wastewater treatment. The method comprises the following steps of (1) associating 2 process systems of magnesium hydroxide and magnesium ammonium sulfate, controlling a part of ammonia water and magnesium sulfate to react to generate a magnesium hydroxide filter material and an ammonium sulfate solution, and converting the filter material into industrial magnesium hydroxide, high-purity magnesite or industrial magnesium oxide; and evaporating, concentrating and crystallizing the ammonium sulfate and the unreacted magnesium sulfate solution to obtain the magnesium ammonium sulfate product. The novel resource utilization method for the joint production of magnesium ammonium sulfate and magnesium hydroxide from the regeneration of magnesium hydroxide from the desulfurization solution magnesium sulfate is completed by the shortest process and the fewest control operations, and the regenerated product has the characteristics of low cost, wide market and high investment benefit, and the resource utilization technology of the desulfurization solution of magnesium method desulfurization is highly innovative, thereby having important practical significance and long-term development significance.
Description
Technical Field
The invention belongs to the technical field of industrial wastewater treatment, and particularly relates to a system for co-production of magnesium hydroxide and magnesium ammonium sulfate by regeneration of desulfurized liquid magnesium sulfate.
Background
The industrial flue gas treatment is developing towards ultra-low and ultra-clean emission. The exhaust emission condition of the purified tail gas is that the purified tail gas after dust removal, denitration and desulfurization meets the ultra-low emission requirement except that ammonia escapes and desulfurization solution escapes and is not temporarily listed in a monitoring range. The desulfurization solid waste treatment condition mainly takes byproduct gypsum formed by calcium desulfurization as a main material, and besides a small amount of solid waste is converted into gypsum primary products in part of inland cities, most areas can only be subjected to landfill treatment nearby due to poor quality and limited market capacity of the desulfurization gypsum solid waste. In the aspect of desulfurization waste water, the condition is not optimistic, has a lot of problems, and it is very essential that these high salt industrial waste water be different from domestic waste water and can handle through sewage treatment system, can only produce the enterprise's oneself by waste water at present and handle, specifically embodies: firstly, wet desulphurization is the main desulphurization process in China, and no matter which process generates a large amount of harmful wastewater with complex components; secondly, the waste water exists in a soluble liquid state, which brings difficulty to environmental protection supervision; thirdly, the treatment technology of the wastewater has a hysteresis condition, and many enterprises do not know how to treat the wastewater; fourthly, many enterprises do not need to invest heavy gold to separate the components of the wastewater and evaporate and crystallize soluble salts in the wastewater, but legal access is difficult to find due to the background of dangerous waste; fifthly, the desulfurization solution of the magnesium desulfurization process can be concentrated and crystallized to obtain magnesium sulfate products, but due to the factors of poor quality, low price, long transportation and the like, a large amount of products are accumulated to form potential soluble solid waste; sixthly, although a plurality of enterprises are matched with a plurality of wastewater treatment and recovery equipment, the enterprises actually do illegal actions of light, dark and dark discharge. The results from these problems are self-evident.
In recent years, the method has a good tendency in the aspect of flue gas magnesium desulphurization resource utilization, and provides some effective treatment means. The measures convert adverse factors into favorable conditions, fully utilize the characteristic of high salt content of the wastewater, promote the waste liquid to the resource height, utilize the energy advantages of desulfurization enterprises, and respectively utilize a plurality of components to perform resource utilization and conversion from low to high, from inferior to excellent, from low price to high added value by means of fine chemical measures, and can show extremely strong profitability, thereby laying a path for industrialized development for the passive cost control in the future to the active money-earning control in the future, and providing powerful technical support for environmental protection and development.
Obviously, based on the point that the desulfurization product magnesium sulfate waste liquid can be converted into a product with high quality, high added value and wide market demand, the great development space of the magnesium desulfurization process and the prospect of modifying other desulfurization processes can be seen completely.
Disclosure of Invention
The invention aims to provide a system for coproducing magnesium ammonium sulfate and magnesium hydroxide from desulfurized liquid magnesium sulfate, which utilizes the characteristic that magnesium sulfate and concentrated ammonia water only can be partially converted and separated to obtain magnesium hydroxide and ammonium sulfate, controls the molecular ratio of ammonium sulfate and magnesium sulfate in the liquid after the reaction by adjusting the adding amount of the concentrated ammonia water, and performs cyclic concentration crystallization to obtain a magnesium ammonium sulfate product, so that the desulfurized liquid magnesium sulfate can be converted into a chemical product with high quality, high benefit and large market demand by the shortest process, and the zero discharge of waste residues and waste water is ensured.
In order to achieve the purpose, the invention provides a system for coproducing magnesium ammonium sulfate and magnesium hydroxide by regenerating magnesium sulfate from desulfurization solution, which only comprises 2 chemical units which are mutually related according to a chemical reaction principle and a chemical reaction process, and is characterized in that:
P1: comprises a purification and impurity removal unit, a concentration adjustment ammonia precipitation unit and a filtration and washing unit in sequence to form industrial magnesium hydroxide Mg (OH)2A product preparation subsystem;
p2: ammonium magnesium sulfate x (NH) is sequentially composed of a multi-effect evaporation concentration unit and a crystallization separation unit4)2SO4.yMgSO4.xH2O product preparation subsystem;
p3: 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 inlet, a concentrated ammonia water inlet and a slurry outlet communicated with the slurry inlet of the filtration washing unit; the filtering and washing unit is also provided with a pure water injection port, a filtrate discharge port, a washing liquid discharge port and a magnesium hydroxide filter material discharge port, the filtrate discharge port is communicated with the feed port of the multi-effect evaporation and concentration unit, the washing liquid discharge port is communicated with the feed port of the concentration adjustment ammonia precipitation unit, and the magnesium hydroxide filter material discharge port is a regenerated magnesium hydroxide product; the ammonium sulfate and magnesium sulfate filtrate after part of the magnesium hydroxide filter material is separated by precipitation is led out from a filtrate outlet of a filtering and washing unit and enters a multi-effect evaporation concentration unit from a feed inlet of the multi-effect evaporation concentration unit communicated with the filtrate outlet, and the multi-effect evaporation concentration unit is also provided with a steam inlet, a condensed water (pure water) outlet, a solution condensed water outlet, a concentrated solution discharge port communicated with the feed inlet of the crystallization separation unit and a mother solution return port communicated with a mother solution discharge port of the crystallization separation unit; the crystallization separation unit is also provided with ammonium magnesium sulfate x (NH)4)2SO4.yMgSO4.xH2O, product outlet; the outlet of the steam condensate (pure water) of the multi-effect evaporation concentration unit is communicated with the pure water inlet of the filtering and washing unit, and the outlet of the solution condensate (solution evaporation condensate) of the multi-effect evaporation concentration unit is communicated with the solution condensate inlet of the concentration adjustment ammonia precipitation unit.
It is worth describing that, in the above system P1 subsystem, the magnesium hydroxide filter material is used to express industrial magnesium hydroxide, and the magnesium hydroxide filter material is mainly used to regenerate magnesium hydroxide based on the low cost, high performance and flexibility, and has advantages of industrial and market value, such as no increase of desulfurization cost when used as a high-quality desulfurizer to return to a magnesium desulfurization system, and also can greatly improve desulfurization efficiency and quality of desulfurization liquid magnesium sulfate, and the magnesium hydroxide filter material can be respectively subjected to low-temperature drying, low-temperature calcination and high-temperature electric melting to obtain industrial magnesium hydroxide, magnesium oxide and high-purity magnesite products.
Therefore, based on the basic scheme, the following optimization technical scheme can be derived:
preferably, a drying unit and a crushing package 1 unit are connected behind the filtering and washing unit of the P1 subsystem, a magnesium hydroxide filter material outlet of the filtering and washing unit is communicated with a material inlet of the drying unit, the drying unit is provided with a combustion gas inlet and a dried material outlet communicated with a material inlet of the crushing package 1 unit, and a material outlet of the packaging and crushing package 1 unit obtains industrial magnesium hydroxide Mg (OH)2And (5) producing the product.
Preferably, the drying unit can be also provided with a dry flue gas outlet for recovering the heat of the flue gas and communicating with the dry flue gas inlet of the scrubbing, concentrating, desulfurizing and dedusting unit.
Preferably, a discharge port of the drying unit of the P1 subsystem can be independently or parallelly connected with a high-temperature electric melting unit and a calcining unit, the discharge port of the high-temperature electric melting unit directly obtains high-purity magnesia MgO, the calcining unit is communicated with a feed port of the crushing and packaging 2 unit except a combustion gas inlet, and the industrial magnesia product MgO is obtained from the discharge port of the packaging and crushing 2 unit.
Based on the fact that filtrate of the filtering and washing unit is ammonium sulfate solution formed by reaction of strong ammonia water and magnesium hydroxide precipitation, unreacted magnesium sulfate solution and heat energy smoke generated by the drying unit or/and the calcining unit, heat exchange is carried out between the ammonium sulfate solution and the unreacted magnesium sulfate solution to evaporate partial water so as to reduce the burden of the multi-effect evaporation and concentration unit, the following technical scheme can be formed:
preferably, a washing concentration desulfurization dust removal unit and a filtering purification unit can be additionally arranged before the multi-effect evaporation concentration unit of the P2 subsystem, the washing concentration desulfurization dust removal unit is provided with a filtrate feeding hole, a drying flue gas and a calcining flue gas pressing-in hole (when only drying flue gas or calcining flue gas exists, the drying flue gas pressure inlet or the calcining flue gas pressure inlet is expressed as a drying flue gas pressure inlet), a clean flue gas exhaust hole and a washing liquid discharge hole, the filtrate feeding hole is communicated with a filtrate discharge hole of the filtering and washing unit of the P1 subsystem, the drying flue gas and calcining flue gas inlet is communicated with a drying flue gas discharge hole of the drying unit of the P1 subsystem or/and a calcining flue gas discharge hole of the calcining unit, and the washing liquid discharge hole is communicated with the feeding hole of the multi-effect evaporation concentration unit.
The mixed solution of ammonium sulfate and magnesium sulfate entering from a filtrate feed inlet of a scrubbing, concentrating, desulfurizing and dedusting unit is reversely exchanged with the higher-temperature sulfur-containing and dust-containing flue gas entering from the lower part of the mixed solution in a spraying mode to complete the desulfurization, scrubbing and concentrating task, the evaporation of water in the solution is promoted, and the mixed solution is discharged from an emptying outlet along with the clean flue gas, so that the ammonium sulfate and magnesium sulfate solution is primarily concentrated, a scrubbing liquid discharge outlet of the mixed solution is communicated with a filter purification unit, the primarily concentrated ammonium sulfate and magnesium sulfate solution is pressed into the filter purification unit, the purified ammonium sulfate and magnesium sulfate solution is led out from a discharge outlet of the filter purification unit and enters a multi-effect evaporation and concentration unit from a feed inlet of the multi-effect evaporation and concentration unit communicated with the filter purification unit, and the multi-effect evaporation and concentration unit is also provided with a steam inlet, a condensed water (pure water) discharge outlet, a solution condensed water discharge outlet, a concentrated solution discharge outlet communicated with a feed inlet of a crystallization separation unit and a mother solution discharge outlet communicated with a mother solution discharge outlet of the concentration and separation unit A liquid return port; the crystallization separation unit is also provided with ammonium magnesium sulfate x (NH)4)2SO4.yMgSO4.xH2O, product outlet; the outlet of the steam condensate (pure water) of the multi-effect evaporation concentration unit is communicated with the pure water inlet of the filtering and washing unit, and the outlet of the solution condensate (solution evaporation condensate) of the multi-effect evaporation concentration unit is communicated with the solution condensate inlet of the concentration adjustment ammonia precipitation unit.
Preferably, under the condition of having the advantage of waste heat wind, a waste heat wind (waste heat air) inlet can be arranged on the P2 gas washing, concentrating, desulfurizing and dedusting unit, the entering waste heat air also carries out reverse heat exchange with the ammonium sulfate solution sprayed from top to bottom, and the waste heat energy is utilized to the maximum extent.
Based on the integrity of the system and the diversified consideration of products, the following technical scheme is formed:
preferably, the drying unit is provided with a dry flue gas outlet and three dry material outlets besides a combustion gas injection port, the dry flue gas outlet is communicated with a flue gas press-in port of the scrubbing, concentrating, desulfurizing and dedusting unit, the three dry material outlets are respectively communicated with a feed port of the crushing and packaging unit 1, a feed port of the high-temperature electric melting unit and a feed port of the calcining unit, a discharge port of the calcining unit is communicated with a feed port of the crushing and packaging unit 2, and the crushing and packaging unit 1 is provided with industrial magnesium hydroxide Mg (OH)2The high-temperature electric melting unit is provided with a high-purity magnesia MgO product discharge port, the crushing package 2 unit is provided with an industrial magnesia MgO product discharge port, and a calcining flue gas discharge port of the calcining unit is also communicated with a flue gas press-in port of the scrubbing, concentrating, desulfurizing and dedusting unit;
the invention provides a system for coproducing magnesium ammonium sulfate and magnesium hydroxide by regenerating magnesium hydroxide from desulfurization solution 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 accumulated periodically to be used as landfill or returned to a fly ash utilization system for utilization. Similarly, the fly ash filtered by the filtration purification unit of the P2 subsystem can be treated as above.
The invention provides a system for coproducing magnesium hydroxide and magnesium ammonium sulfate from desulfurized liquid magnesium sulfate, wherein circulating washing gas is not marked in a washing gas concentration, desulfurization and dust removal unit in a P2 subsystem, and the circulating washing gas is not excluded by the invention.
The combustion gas and the blast furnace gas are the same low-combustion value gas, and the use of gas resources such as coke oven gas and the like is not excluded.
The ammonia water of the invention is generally concentrated ammonia water.
The invention provides a system for coproducing magnesium ammonium sulfate and magnesium hydroxide by regenerating magnesium sulfate from desulfurization liquid, wherein all units of the system can be decomposed or combined as necessary, and the decomposition and combination follow a common chemical reaction principle without forming creative breakthrough to the invention.
The invention provides a system for coproducing magnesium ammonium sulfate and magnesium hydroxide by regenerating magnesium sulfate from desulfurization liquid, which does not exclude the use of other heat sources such as hot air, steam, electric energy and the like except for burning coal gas as a heat source of a drying unit.
The invention provides a system for coproducing magnesium ammonium sulfate and magnesium hydroxide by regenerating magnesium sulfate from desulfurized liquid, which does not exclude the use of other heat sources such as electric energy and the like except for burning coal gas.
The invention provides a system for coproducing magnesium ammonium sulfate and magnesium hydroxide from desulfurized liquid magnesium sulfate, and relates to magnesium ammonium sulfate x (NH)4)2SO4.yMgSO4.xH2O is a double salt product, wherein: x is 2-3, y is 2-3, and z is 5-6.
The quality requirement of magnesium ammonium sulfate is mainly based on the nitrogen content, and is more frequently based on the nitrogen (N)% > 6, so that (NH)4)2SO4.MgSO4.6H2O is a representative structure of magnesium ammonium sulfate, and the nitrogen content of the magnesium ammonium sulfate is more than 7 percent and is easy to achieve.
Compared with the prior art, the invention has the beneficial effects that:
the invention provides a system for co-producing magnesium ammonium sulfate by regenerating magnesium hydroxide from desulfurized liquid magnesium sulfate, which controls the adding speed of concentrated ammonia water, the stirring intensity, the adding total amount and the pH value and the conversion rate of magnesium hydroxide precipitated from partial magnesium sulfate so as to control the molecular number of the magnesium sulfate converted into ammonium sulfate and the molecular number of the residual magnesium sulfate to be in a certain proportion range, and obtains a magnesium hydroxide filter material, industrial magnesium hydroxide, high-purity magnesia and industrial magnesium oxide respectively by washing, drying, electric melting and calcining a separated and regenerated magnesium hydroxide filter cake (filter material), and obtains a magnesium ammonium sulfate product by evaporating, concentrating and crystallizing the filtrate separated from magnesium hydroxide. The resource utilization problem of the desulfurized liquid magnesium sulfate regenerated magnesium hydroxide and magnesium ammonium sulfate is solved by the shortest process and the fewest control operations, and the regenerated product has the characteristics of low cost, wide market and high investment benefit, greatly reduces the risk of desulfurization and the transfer of the desulfurized waste liquid to the resource utilization, and has important practical significance and long-term development significance for the improvement of the desulfurization process and the development of the magnesium desulfurization process in future.
Drawings
The invention 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 invention, and that other drawings can be obtained by those skilled in the art without inventive effort.
FIG. 1 is a schematic diagram of a system for co-production of magnesium ammonium sulfate from magnesium hydroxide regenerated from desulfurized liquid magnesium sulfate according to the present invention.
As can be seen from FIG. 1, the system of the present invention is clear and can be used for intuitively and clearly explaining the content of the present invention.
Fig. 2 is a schematic diagram of the basic characteristic identification of a system for co-producing magnesium ammonium sulfate from desulfurized liquid magnesium sulfate regenerated magnesium hydroxide provided by the invention.
FIG. 3 is a schematic diagram of an optimized feature identifier of a system for co-production of magnesium ammonium sulfate from desulfurized liquid magnesium sulfate regenerated magnesium hydroxide.
Fig. 4 is a specific characteristic identification schematic diagram of a system for co-producing magnesium ammonium sulfate from desulfurized liquid magnesium sulfate regenerated magnesium hydroxide provided by the invention.
In the attached drawings
1-purification and impurity removal unit, 2-concentration adjustment ammonia precipitation unit, 3-filtration and washing unit,
4-drying unit, 5-crushing and packaging 1 unit, 6-high temperature electric melting unit,
7-calcining unit, 8-pulverizing and packaging 2 unit, 9-scrubbing, concentrating, desulfurizing and dedusting unit,
10-filtration purification unit, 11-multiple-effect evaporation concentration unit and 12-crystallization separation unit.
Detailed Description
Example 1: as can be seen from fig. 2, the present invention provides a basic characteristic implementation manner of a system for co-producing magnesium ammonium sulfate from desulfurized liquid magnesium sulfate regenerated magnesium hydroxide, which is composed of 2 chemical units in a mutual correlation manner according to a chemical reaction principle and a chemical reaction process, and is characterized in that:
p1: comprises a purification and impurity removal unit, a concentration adjustment ammonia precipitation unit and a filtration and washing unit in sequence to form industrial magnesium hydroxide Mg (OH)2A product preparation subsystem;
p2: ammonium magnesium sulfate x (NH) is sequentially composed of a multi-effect evaporation concentration unit and a crystallization separation unit4)2SO4.yMgSO4.xH2O product preparation subsystem;
p3: 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 inlet, a concentrated ammonia water inlet and a slurry outlet communicated with the slurry inlet of the filtration washing unit; the filtering and washing unit is also provided with a pure water injection port, a filtrate discharge port, a washing liquid discharge port and a magnesium hydroxide filter material discharge port, the filtrate discharge port is communicated with the feed port of the multi-effect evaporation and concentration unit, the washing liquid discharge port is communicated with the feed port of the concentration adjustment ammonia precipitation unit, and the magnesium hydroxide filter material discharge port is a regenerated magnesium hydroxide product; the ammonium sulfate and magnesium sulfate filtrate after part of the magnesium hydroxide filter material is separated by precipitation is led out from a filtrate outlet of a filtering and washing unit and enters a multi-effect evaporation concentration unit from a filtrate inlet of the multi-effect evaporation concentration unit communicated with the filtrate outlet, and the multi-effect evaporation concentration unit is also provided with a steam inlet, a condensed water (pure water) outlet, a solution condensed water outlet, a concentrated solution outlet communicated with the feed inlet of the crystallization separation unit and a mother solution return port communicated with a mother solution outlet of the crystallization separation unit; the crystallization separation unit is also provided with ammonium magnesium sulfate x (NH)4)2SO4.yMgSO4.xH2O, product outlet; multi-effect evaporation concentration unitThe pure water outlet is connected to the pure water inlet of the filtering and washing unit, and the solution condensed water outlet of the multi-effect evaporation and concentration unit is connected to the solution condensed water inlet of the concentration-adjusting ammonia precipitation unit.
Example 2: as can be seen from fig. 3, the present invention provides an optimized characteristic implementation manner of a system for co-producing magnesium ammonium sulfate from desulfurized liquid magnesium sulfate regenerated magnesium hydroxide, which is composed of only 2 chemical units in accordance with the chemical reaction principle and process, and is characterized in that:
p1: the industrial magnesium hydroxide Mg (OH) consists of a purification and impurity removal unit, a concentration adjustment ammonia precipitation unit and a filtration and washing unit in sequence2A product preparation subsystem; the utility model is characterized in that: the discharge port of the magnesium hydroxide filter material of the filtering and washing unit is also communicated with a drying unit and a crushing and packaging unit 1;
p2: ammonium magnesium sulfate x (NH) is sequentially composed of a multi-effect evaporation concentration unit and a crystallization separation unit4)2SO4·yMgSO4·xH2O product preparation subsystem; the utility model is characterized in that: the front end of the multi-effect evaporation concentration unit is also communicated with a gas washing concentration desulfurization dust removal unit and a filtering purification unit;
p3: the purifying and impurity removing unit consists of a desulfurizing liquid MgSO4Feed inlet and cleaned MgSO4The solution discharge port is communicated with the feed port 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 inlet, a concentrated ammonia water inlet and a slurry outlet communicated with the slurry inlet of the filtration washing unit; the filtering and washing unit is also provided with a pure water injection port, a filtrate discharge port, a washing liquid discharge port and a magnesium hydroxide filter material discharge port, wherein the washing liquid discharge port is communicated with the washing liquid feeding port of the concentration adjusting ammonia precipitation unit, and the magnesium hydroxide filter material discharge port is communicated with the feeding port of the drying unit; the drying unit is also provided with a combustion gas inlet, a drying flue gas outlet and a discharge hole communicated with the feed inlet of the crushing package 1 unit; the crushing package 1 unit is also provided with a discharge port for collecting industrial magnesium hydroxide products; the filtrate outlet of the filtering and washing unit is connected with the filtrate inlet of the scrubbing, concentrating, desulfurizing and dedusting unitCommunicating; the gas washing concentration desulfurization dust removal unit is also provided with a dry smoke pressure inlet, a gas washing completion liquid outlet and a clean smoke exhaust port, dry smoke enters the gas washing concentration desulfurization dust removal unit from a bottom dry smoke pressure inlet and is reversely exchanged with filtrate entering from an upper filtrate inlet, and the gas washing completion liquid outlet is communicated with a filter purification unit inlet; the filtering and purifying unit is also provided with a discharge hole communicated with a feed inlet of the multi-effect evaporation and concentration unit; the multi-effect evaporation concentration unit is also provided with a steam inlet, a condensed water (pure water) outlet, a solution condensed water outlet, a concentrated solution outlet communicated with the feed inlet of the crystallization separation unit and a mother solution return port communicated with the mother solution outlet of the crystallization separation unit; the crystallization separation unit is also provided with ammonium magnesium sulfate x (NH)4)2SO4·yMgSO4·xH2O, product outlet; the pure water outlet of the multi-effect evaporation concentration unit is communicated with the pure water inlet of the filtration washing unit, and the solution condensate outlet of the multi-effect evaporation concentration unit is communicated with the solution condensate inlet of the concentration adjustment ammonia precipitation unit.
Example 3: as can be seen from fig. 4, the present invention provides a specific characteristic implementation manner of a system for co-producing magnesium ammonium sulfate from desulfurized liquid magnesium sulfate regenerated magnesium hydroxide, which is composed of 2 chemical units in a mutual correlation manner according to a chemical reaction principle and a chemical reaction process, and is characterized in that:
p1: comprises a purification and impurity removal unit, a concentration adjustment ammonia precipitation unit, a filtration and washing unit, a drying unit and a crushing and packaging unit 1 in sequence to form industrial magnesium hydroxide Mg (OH)2A product preparation subsystem; more characterized in that except one dry material discharge port of three drying units is communicated with the feed port of the crushing package 1 unit, the other two dry material discharge ports are respectively communicated with the feed port of the high-temperature electric melting unit and the feed port of the calcining unit, the discharge port of the calcining unit is communicated with the feed port of the crushing package 2 unit, and the crushing package 1 unit is provided with industrial magnesium hydroxide Mg (OH)2A product discharge port, a high-temperature electric melting unit provided with a high-purity magnesia MgO product discharge port, a crushing package 2 unit provided with an industrial magnesia MgO product discharge port, and a calcining unit calcining flue gas discharge port and a drying flue gas discharge port are the sameThe sample is communicated with a flue gas press-in opening of a scrubbing, concentrating, desulfurizing and dedusting unit;
p2: ammonium magnesium sulfate x (NH) is sequentially composed of a scrubbing, concentrating, desulfurizing and dedusting unit, a filtering and purifying unit, a multi-effect evaporation and concentration unit and a crystallization and separation unit4)2SO4.yMgSO4A product preparation subsystem of xH 2O;
p3: 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 inlet, a concentrated ammonia water inlet and a slurry outlet communicated with the slurry inlet of the filtration washing unit; the filtering and washing unit is also provided with a pure water injection port, a filtrate discharge port, a washing liquid discharge port and a magnesium hydroxide filter material discharge port, wherein the washing liquid discharge port is communicated with the washing liquid feeding port of the concentration adjustment ammonia precipitation unit, and the magnesium hydroxide filter material discharge port is communicated with the feed port of the drying unit; the drying unit is also provided with a combustion gas inlet, a drying flue gas outlet, a discharge hole communicated with the feed inlet of the crushing and packaging unit 1 and a discharge hole communicated with the feed inlet of the high-temperature electric melting unit or/and the feed inlet of the calcining unit; the discharge hole of the calcining unit is also communicated with the feed hole of the unit crushing and packaging 2; the crushing package 1 unit is provided with a discharge hole for collecting industrial magnesium hydroxide products; the discharge hole of the high-temperature electric melting unit is used for collecting high-purity magnesia; the discharge port of the unit of the crushing package 2 is used for collecting industrial magnesium oxide; the calcining unit is provided with a combustion gas inlet, a calcining flue gas outlet and a discharge port communicated with the feed port of the crushing and packaging unit 2, and the calcining flue gas outlet is communicated with the drying flue gas outlet in parallel and communicated with a drying flue gas press-in port of the scrubbing, concentrating, desulfurizing and dedusting unit; a filtrate outlet of the filtering and washing unit is communicated with a filtrate inlet of the scrubbing, concentrating, desulfurizing and dedusting unit; the scrubbing concentration desulfurization dust removal unit is also provided with a dry smoke pressure inlet, a scrubbing completion liquid outlet and a clean smoke exhaust port, dry smoke enters the scrubbing concentration desulfurization dust removal unit from the bottom dry smoke pressure inlet and is reversely exchanged with filtrate entering from the upper filtrate inlet, and the scrubbing completion liquid outlet and the purification filtration unit are arrangedThe element feed inlets are communicated; the filtering and purifying unit is also provided with a discharge hole communicated with a feed inlet of the multi-effect evaporation and concentration unit; the multi-effect evaporation concentration unit is also provided with a steam inlet, a condensed water (pure water) outlet, a solution condensed water outlet, a concentrated solution outlet communicated with the feed inlet of the crystallization separation unit and a mother solution return port communicated with the mother solution outlet of the crystallization separation unit; the crystallization separation unit is also provided with ammonium magnesium sulfate x (NH)4)2SO4.yMgSO4.xH2O, product outlet; the pure water outlet of the multi-effect evaporation concentration unit is communicated with the pure water inlet of the filtering and washing unit, and the solution condensate outlet of the multi-effect evaporation concentration unit is communicated with the solution condensate inlet of the concentration-adjusting ammonia precipitation unit.
Claims (3)
1. The utility model provides a desulfurization liquid magnesium sulfate regeneration magnesium hydroxide coproduction magnesium ammonium sulfate magnesium system, only by 2 chemical industry units according to chemical industry reaction principle and process interrelatedly, its characterized in that:
p1: comprises a purification and impurity removal unit (1), a concentration adjustment ammonia precipitation unit (2) and a filtration and washing unit (3) in sequence to form industrial magnesium hydroxide Mg (OH)2A product preparation subsystem;
p2: ammonium magnesium sulfate x (NH) is sequentially composed of a multi-effect evaporation concentration unit (11) and a crystallization separation unit (12)4)2SO4.yMgSO4.xH2O product preparation subsystem;
p3: 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 inlet, a concentrated ammonia water inlet and a slurry outlet communicated with the slurry inlet of the filtration washing unit (3); the filtering and washing unit (3) is also provided with a pure water filling opening, a filtrate discharging opening, a washing liquid discharging opening and a magnesium hydroxide filter material discharging opening, the filtrate discharging opening is communicated with the feeding opening of the multi-effect evaporation and concentration unit (11), the washing liquid discharging opening is communicated with the feeding opening of the concentration adjustment ammonia precipitation unit (2), and the magnesium hydroxide filter material discharging opening is regeneratedA magnesium hydroxide product; the ammonium sulfate and magnesium sulfate filtrate after part of the magnesium hydroxide filter material is separated by precipitation is led out from a filtrate outlet of the filtering and washing unit (3) and enters the multi-effect evaporation and concentration unit (11) from a filtrate inlet of the multi-effect evaporation and concentration unit (11) communicated with the filtrate outlet, and the multi-effect evaporation and concentration unit (11) is also provided with a steam inlet, a condensed water outlet, a solution condensed water outlet, a concentrated solution outlet communicated with the feed inlet of the crystallization and separation unit (12) and a mother solution return port communicated with a mother solution outlet of the crystallization and separation unit (12); the crystallization separation unit (12) is also provided with magnesium ammonium sulfate x (NH)4)2SO4.yMgSO4.xH2O, product outlet; the pure water outlet of the multi-effect evaporation concentration unit (11) is communicated with the pure water inlet of the filtering and washing unit (3), and the solution condensate outlet of the multi-effect evaporation concentration unit (11) is communicated with the solution condensate inlet of the concentration adjustment ammonia precipitation unit (2).
2. The system for co-production of magnesium ammonium sulfate from magnesium hydroxide regenerated from desulfurized liquid magnesium sulfate according to claim 1, wherein: the magnesium hydroxide filter material outlet of the filtering and washing unit (3) is also communicated with a drying unit (4) and a crushing and packaging unit (5) 1; the front end of the multi-effect evaporation concentration unit (11) is also communicated with a gas washing concentration desulfurization dust removal unit (9) and a filtering purification unit (10);
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 inlet, a concentrated ammonia water inlet and a slurry outlet communicated with the slurry inlet of the filtration washing unit; the filtering and washing unit (3) is also provided with a pure water filling opening, a filtrate discharging opening, a washing liquid discharging opening and a magnesium hydroxide filter material discharging opening, the washing liquid discharging opening is communicated with the washing liquid adding opening of the concentration adjustment ammonia precipitation unit (2), and the magnesium hydroxide filter material discharging opening is communicated with the feeding opening of the drying unit (4); the drying unit (4) is also provided with a combustion gas inlet, a drying smoke outlet and a discharge hole communicated with the feed inlet of the unit (5) of the crushing package 1; crush pack 1The unit (5) is also provided with a discharge hole for collecting industrial magnesium hydroxide products; a filtrate outlet of the filtering and washing unit (3) is communicated with a filtrate inlet of the scrubbing, concentrating, desulfurizing and dedusting unit (9); the scrubbing concentration desulfurization dust removal unit (9) is also provided with a dry smoke pressure inlet, a scrubbing completion liquid outlet and a clean smoke exhaust port, dry smoke enters the scrubbing concentration desulfurization dust removal unit (9) from a bottom dry smoke pressure inlet and reversely exchanges with filtrate entering from an upper filtrate inlet, and the scrubbing completion liquid outlet is communicated with a feed inlet of the filtering and purifying unit (10); the filtering and purifying unit (10) is also provided with a discharge hole communicated with a feed hole of the multi-effect evaporation and concentration unit (11); the multi-effect evaporation concentration unit (11) is also provided with a steam inlet, a condensed water outlet, a solution condensed water outlet, a concentrated solution outlet communicated with the feed inlet of the crystallization separation unit (12) and a mother solution return port communicated with the mother solution outlet of the crystallization separation unit (12); the crystallization separation unit (12) is also provided with magnesium ammonium sulfate x (NH)4)2SO4.yMgSO4.xH2O, product outlet; the pure water outlet of the multi-effect evaporation concentration unit (11) is communicated with the pure water inlet of the filtering and washing unit (3), and the solution condensate outlet of the multi-effect evaporation concentration unit (11) is communicated with the solution condensate inlet of the concentration adjustment ammonia precipitation unit (2).
3. The system for the co-production of magnesium ammonium sulfate from the regeneration of magnesium hydroxide by desulfurized liquid magnesium sulfate according to claim 1 or 2, characterized in that: except that one of the three drying units (4) is communicated with the feed inlet of the crushing package 1 unit (5) at the material discharge port, the other two drying material discharge ports are also respectively communicated with the feed inlet of the high-temperature electric melting unit (6) and the feed inlet of the calcining unit (7), the discharge port of the calcining unit (7) is communicated with the feed inlet of the crushing package 2 unit (8), and the crushing package 1 unit (5) is provided with industrial magnesium hydroxide Mg (OH)2A product discharge port, a high-temperature electric melting unit (6) is provided with a high-purity magnesia MgO product discharge port, a crushing package 2 unit (8) is provided with an industrial magnesia MgO product discharge port, and a calcining flue gas discharge port of a calcining unit (7) is communicated with a drying flue gas discharge port and communicated with a flue gas press-in port of a scrubbing, concentrating, desulfurizing and dedusting unit (9);
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 inlet, a concentrated ammonia water inlet and a slurry outlet communicated with the slurry inlet of the filtration washing unit (3); the filtering and washing unit (3) is also provided with a pure water filling opening, a filtrate discharging opening, a washing liquid discharging opening and a magnesium hydroxide filter material discharging opening, the washing liquid discharging opening is communicated with the washing liquid adding opening of the concentration adjustment ammonia precipitation unit (2), and the magnesium hydroxide filter material discharging opening is communicated with the feeding opening of the drying unit (4); the drying unit (4) is also provided with a combustion gas inlet, a drying flue gas outlet, a discharge hole communicated with the feed inlet of the unit (5) of the crushing package 1, and a discharge hole communicated with the feed inlet of the high-temperature electric melting unit (6) or/and the feed inlet of the calcining unit (7); the discharge hole of the calcining unit (7) is also communicated with the feed hole of the crushing package 2 unit (8); the crushing package 1 unit (5) is provided with a discharge hole for collecting industrial magnesium hydroxide products; the discharge hole of the high-temperature electric melting unit (6) is used for collecting high-purity magnesia; the discharge port of the unit (8) of the crushing package 2 is used for collecting industrial magnesium oxide; the calcining unit (7) is provided with a combustion gas inlet, a calcining flue gas outlet and a discharge hole communicated with the feed inlet of the crushing package 2 unit (8), and the calcining flue gas outlet is communicated with the dry flue gas outlet in parallel and communicated with a dry flue gas press-in opening of the scrubbing, concentrating, desulfurizing and dedusting unit (9); a filtrate outlet of the filtering and washing unit (3) is communicated with a filtrate inlet of the scrubbing, concentrating, desulfurizing and dedusting unit (9); the scrubbing concentration desulfurization dust removal unit (9) is also provided with a dry smoke pressure inlet, a scrubbing completion liquid outlet and a clean smoke exhaust port, dry smoke enters the scrubbing concentration desulfurization dust removal unit (9) from a bottom dry smoke pressure inlet and reversely exchanges with filtrate entering from an upper filtrate inlet, and the scrubbing completion liquid outlet is communicated with a feed inlet of the filtering and purifying unit (10); the filtering and purifying unit (10) is also provided with a discharge hole communicated with a feed hole of the multi-effect evaporation and concentration unit (11); the multi-effect evaporation concentration unit (11) is also provided with a steam inlet, a condensed water outlet, a solution condensed water outlet and a concentrated solution outlet communicated with the feed inlet of the crystallization separation unit (12)The port is communicated with a mother liquor return port communicated with a mother liquor discharge port of the crystallization separation unit (12); the crystallization separation unit (12) is also provided with magnesium ammonium sulfate x (NH)4)2SO4.yMgSO4.xH2O, product outlet; the pure water outlet of the multi-effect evaporation concentration unit (11) is communicated with the pure water inlet of the filtering and washing unit (3), and the solution condensate outlet of the multi-effect evaporation concentration unit (11) is communicated with the solution condensate inlet of the concentration adjustment ammonia precipitation unit (2).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121822166.3U CN216005237U (en) | 2021-07-30 | 2021-07-30 | System for coproduction of magnesium hydroxide and magnesium ammonium sulfate from desulfurization liquid magnesium sulfate |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121822166.3U CN216005237U (en) | 2021-07-30 | 2021-07-30 | System for coproduction of magnesium hydroxide and magnesium ammonium sulfate from desulfurization liquid magnesium sulfate |
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