CN204550082U - Prepare the equipment of high-purity anhydrous sodium sulfate and feedwater - Google Patents
Prepare the equipment of high-purity anhydrous sodium sulfate and feedwater Download PDFInfo
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- CN204550082U CN204550082U CN201520111084.6U CN201520111084U CN204550082U CN 204550082 U CN204550082 U CN 204550082U CN 201520111084 U CN201520111084 U CN 201520111084U CN 204550082 U CN204550082 U CN 204550082U
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Abstract
The utility model relates to a kind of equipment preparing high-purity anhydrous sodium sulfate and feedwater, comprise the first preheater, first reactor, second reactor, film filter, second preheater and hot pressing nitre tank, hot pressing nitre tank is provided with vapour outlet and the outlet of nitre slurry, vapour outlet connects the opening for feed of steam washer, the discharge port of steam washer connects the opening for feed of vapour compressor, the discharge port connecting vapour compressor connects the opening for feed of desuperheater, the discharge port of desuperheater is connected with the heating chamber of hot pressing nitre tank, the nitre slurry outlet of hot pressing nitre tank connects whizzer opening for feed, discharge hole of centrifugal machine connects drying bed, drying bed connects wrapping machine.Adopt more energy-saving and cost-reducing new installation, technique comparatively multiple-effect evaporation technology is simple, and production energy consumption is low, only has about 75% of multiple-effect evaporation.Constant product quality, purity is high, can reach more than 99.4%.The energy consumption of not only producing reduces, and improves quality product.
Description
Technical field
The utility model relates to inorganic salt preparing technical field, especially a kind of equipment preparing high-purity anhydrous sodium sulfate and feedwater.
Background technology
Putting forward nitre technique at present has two kinds: one to be cold process, and two is hot methods.Cold process process, constant product quality, but it also has shortcoming: investment is comparatively large, energy consumption is high, refrigeration system seriously corroded etc., because freezing being over is ten water nitre, also need to adopt scorification, melting+method of evaporation, salting-out process or complete molten method of evaporation to obtain anhydrous sodium sulphate, cold process technical matters is complicated, long flow path, energy consumption is high to be just progressively eliminated; Hot rule is just contrary with cold process, and with multiple-effect vacuum evaporation pump circulation nitre technique for representative, the vanguard technology that wherein external heat five imitates pump circulation vacuum nitre becomes first-selection.
Five effect vacuum-evaporation adverse current feeding production technique have been widely used in thenardite production.Because glauberite contains sodium sulfate is low, adopt the glass gall concentration that obtains of water soluble method low, so need with the large vaporizer of heat interchanging area.In order to make full use of heat, adopt adverse current feeding.This method production technique is rigorous, and vacuum unit adopts secondary steam, and one-level water sprays, and vacuum tightness can reach more than 0.09MPa; Employing adds two alkali delimings, magnesium, except insolubles in inclined plate settler, then through sand filters, obtains refining glass gall, last stage dust employing hydrometallurgic recovery; Secondary steam, condensed water heat reclaim and are all rationally applied.The advantage of this production technique is that coal consumption is lower, and roughly at about 200kg/t, production cost is low.Current this technique has been promoted in the whole nation and has been adopted, and the anhydrous sodium sulphate purity of this technique output is 98 ~ 99%.Adopt two alkaline purification techniques (production technique of caustic soda demagging, soda ash deliming) although can quality product be ensured, the problem such as also exist that caustic soda, soda ash consumption are large, magnesium hydroxide is difficult to sedimentation and product cost is high.Multiple-effect evaporation is the temperature ensureing last evaporator, and the remaining secondary steam of end effect still has a large amount of heat energy, directly discharges, not only cause a large amount of thermosteresis, and need a large amount of water coolants after cooling.
Reducing discharging requirement in order to adapt to country to nitre industry energy-saving processed, how steam saving cost, raising heating efficiency, is the problem that the industry of current use evaporation concentration is the most urgently paid close attention to.In recent years, MVR technology has become the energy-conserving and emission-cutting technology that all kinds of industry evaporation concentration links such as chemical industry, food-processing industry, salt industry vigorously promote the use, its less energy-consumption, high efficiency feature are obviously better than traditional evaporation technique, have huge development potentiality in future.And precedent is applied in the independent research that nitre industry processed there is no this technology, there is wide opportunity to develop.
Utility model content
The technical problems to be solved in the utility model is: in order to solve, existing nitre equipment energy consumption processed is high, efficiency is low, the problem of time-consuming, provides a kind of equipment preparing high-purity anhydrous sodium sulfate and feedwater.
The utility model solves the technical scheme that its technical problem adopts: a kind of equipment preparing high-purity anhydrous sodium sulfate and feedwater, comprise the first preheater, first reactor, second reactor, film filter, second preheater and hot pressing nitre tank, the discharge port of the first preheater connects the opening for feed of the first reactor, the opening for feed of clear liquor outlet connection second reactor of the first reactor, the opening for feed of the clear liquor outlet junctional membrane strainer of the second reactor, the discharge port of film filter connects the opening for feed of the second preheater, the discharge port of the second preheater connects the opening for feed of hot pressing nitre tank, former glass gall enters the first reactor by mining area after the first preheater heats, salkali waste and settling agent is added to the first reactor, supernatant liquid is exported by the first reactor clear liquor and enters the second reactor, boiler waste gas is passed into the second reactor, second reactor clear liquor enters film filter filters solid suspended substance, after film filter filtering separation, refining glass gall enters nitre autoclave processed after the second preheater heating, described hot pressing nitre tank is provided with vapour outlet and the outlet of nitre slurry, described vapour outlet is connected with steam washer, the discharge port of described steam washer is connected with vapour compressor, the discharge port of described vapour compressor is connected with desuperheater, the discharge port of described desuperheater is connected with the heating chamber of hot pressing nitre tank, after hot pressing nitre tank produces enough secondary steams, just inactive raw steam, the secondary steam that hot pressing nitre tank produces enters vapour compressor compression after steam washer washing, produce the superheated vapour of High Temperature High Pressure, by desuperheater desuperheat to saturated, for glass gall in the oven heats tank of hot pressing nitre tank, feed liquid boiling in nitre autoclave processed after heating, evaporation, produce secondary steam, continue washing, compression, heating, evaporation, circulate and so forth, so when normally producing, do not need to use raw steam, only need to consume electric energy, the nitre slurry outlet of described hot pressing nitre tank is connected with whizzer, described discharge hole of centrifugal machine is connected with drying bed, the discharge port of described drying bed is connected with wrapping machine, drying bed is delivered to by belt conveyor after hot pressing nitre tank row nitre slurry enters centrifuge dewatering, through wrapping machine packaging warehouse-in after drying.
The suspended solid outlet of described first reactor and the suspended solid outlet of the second reactor are connected with pressure filter, and the salt slurry that the first reactor and the second reactor produce is after pressure filter press filtration, and salt slurry returns ore deposit note well.
Described hot pressing nitre tank is also provided with mother liquor outlet, and described mother liquor outlet is connected with the opening for feed of the first reactor, glass gall in nitre autoclave processed after sufficient crystallising mother liquor go to first reactor purification.
The opening for feed getting rid of rear liquid outlet connection hot pressing nitre tank of described whizzer, the rear liquid pump backheat compacting nitre tank that gets rid of after centrifuge dewatering can be used for evaporative crystallization.
The described heating chamber of hot pressing nitre tank is communicated with the heating chamber of the second preheater with the heating chamber of the first preheater, the water of condensation that evaporation produces is used for the former glass gall of the first preheater preheats and the second preheater preheats refines glass gall, not only reclaim heat, and improve the reaction efficiency of former glass gall, save the purification time.
The heating chamber condensing water conduit of the described heating chamber condensing water conduit of hot pressing nitre tank, the heating chamber condensing water conduit of the first preheater and the second preheater is connected with boiler of power plant, because secondary steam washs through steam washer, its purity is higher, the condensed water of condensation of heat exchange delivers to boiler of power plant after cooling, directly as boiler feed water, eliminate the huge and water treatment system of complexity.
The exhaust steam passage of described boiler of power plant connects the opening for feed of the second reactor, and in the second reactor, pass into boiler waste gas, caustic soda carburizing reagent obtains soda ash, the calcium in removing solution.
Add caustic soda and a small amount of settling agent to the first reactor, react with magnesium ion the magnesium hydrate precipitate generating more indissoluble, because the settling agent added has help heavy and adsorptive power, cotton-shaped magnesium hydroxide can well be removed; Then in the second reactor, pass into boiler waste gas, caustic soda carburizing reagent obtains soda ash, the calcium in removing solution.Its reaction formula is as follows:
Reaction 1:
MgSO
4+2NaOH＝Mg(OH)
2↓+Na
2SO
4
Reaction 2:
2NaOH+CO
2(boiler waste gas)=Na
2cO
3+ H
2o
CaSO
4+Na
2CO
3＝Na
2SO
4+CaCO
3↓
Use film filter filters, not only avoid adding flocculation agent and introduce new impurity, solve interpolation flocculation agent and need the time of natural subsidence length, inefficient problem, and ensure the precision of filtering glass gall, wherein suspended solid can control at 0.5mg/L, for the evaporative crystallization of follow-up high-quality nitre provides guarantee.
The beneficial effects of the utility model are, vapour compressor and hot pressing nitre tank are formed the vapo(u)rization system of association, to realize secondary steam heat recovery.The dilute solution of low temperature enters hot pressing nitre tank and concentrates after the first preheater and the second preheater preheats, and secondary steam compresses through compressor, improves pressure, temperature and heat enthalpy value, then sends back in hot pressing nitre tank heating chamber, as heating steam by steam after compression.Become secondary steam again after being absorbed its latent heat by evaporation feed liquid, the latter enters vapour compressor compression again, and so constantly circulation, is converted into high-temperature position heat energy by a large amount of low-temperature heat energy and is used, thus saves a large amount of raw steam, reaches the object of energy-saving consumption-reducing.Adopt salkali waste to replace lime, reclaim and absorb boiler of power plant waste gas, effectively provide cost savings, solve the problems such as two alkaline purification working costs energy consumption that is higher, evaporative crystallization is higher, flow process is longer, complex process.This equipment good economy performance, comprehensive energy consumption is low, and quality product is high, and waste gas is well utilized, and turns waste into wealth, and has purified again environment.
Accompanying drawing explanation
Below in conjunction with drawings and Examples, the utility model is further illustrated.
Fig. 1 is structure diagram of the present utility model.
Embodiment
By reference to the accompanying drawings the utility model is described in further detail now.These accompanying drawings are the schematic diagram of simplification, only basic structure of the present utility model are described in a schematic way, and therefore it only shows the formation relevant with the utility model.
A kind of equipment preparing high-purity anhydrous sodium sulfate and feedwater as shown in Figure 1, comprise the first preheater, first reactor, second reactor, film filter, second preheater and hot pressing nitre tank, the discharge port of the first preheater connects the opening for feed of the first reactor, the opening for feed of clear liquor outlet connection second reactor of the first reactor, the opening for feed of the clear liquor outlet junctional membrane strainer of the second reactor, the discharge port of film filter connects the opening for feed of the second preheater, the discharge port of the second preheater connects the opening for feed of hot pressing nitre tank, described hot pressing nitre tank is provided with vapour outlet and the outlet of nitre slurry, described vapour outlet is connected with steam washer, the discharge port of described steam washer is connected with vapour compressor, the discharge port of described vapour compressor is connected with desuperheater, the discharge port of described desuperheater is connected with the heating chamber of hot pressing nitre tank, the nitre slurry outlet of described hot pressing nitre tank is connected with whizzer, described discharge hole of centrifugal machine is connected with drying bed, the discharge port of described drying bed is connected with wrapping machine.The suspended solid outlet of the first reactor and the suspended solid outlet of the second reactor are connected with pressure filter.Described hot pressing nitre tank is also provided with mother liquor outlet, and described mother liquor outlet is connected with the opening for feed of the first reactor.The opening for feed getting rid of rear liquid outlet connection hot pressing nitre tank of described whizzer.The heating chamber of hot pressing nitre tank is communicated with the heating chamber of the second preheater with the heating chamber of the first preheater.The heating chamber condensing water conduit of hot pressing nitre tank, the heating chamber condensing water conduit of the first preheater are connected boiler of power plant with the heating chamber condensing water conduit of the second preheater.The exhaust steam passage of boiler of power plant connects the opening for feed of the second reactor.
Former glass gall enters the first reactor by mining area after the first preheater heats, salkali waste and settling agent is added to the first reactor, supernatant liquid is exported by the first reactor clear liquor and enters the second reactor, pass into boiler waste gas to the second reactor, the second reactor clear liquor enters film filter filters solid suspended substance.The salt slurry that first reactor and the second reactor produce is after pressure filter press filtration, and salt slurry returns ore deposit note well.After film filter filtering separation, refining glass gall enters nitre autoclave processed after the second preheater heating, and in nitre autoclave processed, after sufficient crystallising, mother liquor goes to the first reactor purification.Drying bed is delivered to by belt conveyor, through wrapping machine packaging warehouse-in after drying after hot pressing nitre tank row nitre slurry enters centrifuge dewatering.Rear liquid pump backheat of getting rid of after centrifuge dewatering suppresses nitre tank for evaporative crystallization.
Whole nitre system processed, only having during driving uses the raw steam of part to carry out preheating, after hot pressing nitre tank produces enough secondary steams, just inactive raw steam, the secondary steam that hot pressing nitre tank produces enters vapour compressor compression after steam washer washing, produce the superheated vapour of High Temperature High Pressure, by desuperheater desuperheat to saturated, for glass gall in the oven heats tank of hot pressing nitre tank.Feed liquid boiling after heating, evaporation, produce secondary steam, continues washing, compression, heating, evaporation, circulate and so forth.So, when normally producing, be do not need to use raw steam, only need to consume electric energy.
The water of condensation that evaporation produces is used for the former glass gall of the first preheater preheats and the second preheater preheats refines glass gall, has not only reclaimed heat, and has improve the reaction efficiency of former glass gall, saved the purification time.Because secondary steam washs through steam washer, its purity is higher, and the condensed water of condensation of heat exchange delivers to boiler of power plant after cooling, directly as boiler feed water, eliminates the huge and water treatment system of complexity.
With above-mentioned according to desirable embodiment of the present utility model for enlightenment, by above-mentioned description, relevant staff in the scope not departing from this utility model technological thought, can carry out various change and amendment completely.The technical scope of this utility model is not limited to the content on specification sheets, must determine its technical scope according to right.
Claims (7)
1. prepare the equipment of high-purity anhydrous sodium sulfate and feedwater for one kind, it is characterized in that: comprise the first preheater, first reactor, second reactor, film filter, second preheater and hot pressing nitre tank, the discharge port of the first preheater connects the opening for feed of the first reactor, the opening for feed of clear liquor outlet connection second reactor of the first reactor, the opening for feed of the clear liquor outlet junctional membrane strainer of the second reactor, the discharge port of film filter connects the opening for feed of the second preheater, the discharge port of the second preheater connects the opening for feed of hot pressing nitre tank, described hot pressing nitre tank is provided with vapour outlet and the outlet of nitre slurry, described vapour outlet is connected with steam washer, the discharge port of described steam washer is connected with vapour compressor, the discharge port of described vapour compressor is connected with desuperheater, the discharge port of described desuperheater is connected with the heating chamber of hot pressing nitre tank, the nitre slurry outlet of described hot pressing nitre tank is connected with whizzer, described discharge hole of centrifugal machine is connected with drying bed, the discharge port of described drying bed is connected with wrapping machine.
2. the equipment of the high-purity anhydrous sodium sulfate of preparation as claimed in claim 1 and feedwater, is characterized in that: the suspended solid outlet of described first reactor and the suspended solid outlet of the second reactor are connected with pressure filter.
3. the equipment of the high-purity anhydrous sodium sulfate of preparation as claimed in claim 1 and feedwater, is characterized in that: described hot pressing nitre tank is also provided with mother liquor outlet, and described mother liquor outlet is connected with the opening for feed of the first reactor.
4. the equipment of the high-purity anhydrous sodium sulfate of preparation as claimed in claim 1 and feedwater, is characterized in that: the opening for feed getting rid of rear liquid outlet connection hot pressing nitre tank of described whizzer.
5. the equipment of the high-purity anhydrous sodium sulfate of preparation as claimed in claim 1 and feedwater, is characterized in that: the described heating chamber of hot pressing nitre tank is communicated with the heating chamber of the second preheater with the heating chamber of the first preheater.
6. the equipment of the high-purity anhydrous sodium sulfate of preparation as claimed in claim 5 and feedwater, it is characterized in that: also comprise boiler of power plant, the described heating chamber condensing water conduit of hot pressing nitre tank, the heating chamber condensing water conduit of the first preheater are connected boiler of power plant with the heating chamber condensing water conduit of the second preheater.
7. the equipment of the high-purity anhydrous sodium sulfate of preparation as claimed in claim 6 and feedwater, is characterized in that: the exhaust steam passage of described boiler of power plant connects the opening for feed of the second reactor.
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|---|---|---|---|
| CN201520111084.6U CN204550082U (en) | 2015-02-15 | 2015-02-15 | Prepare the equipment of high-purity anhydrous sodium sulfate and feedwater |
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|---|---|---|---|
| CN201520111084.6U CN204550082U (en) | 2015-02-15 | 2015-02-15 | Prepare the equipment of high-purity anhydrous sodium sulfate and feedwater |
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