CN204185249U - A kind for the treatment of unit of abraum salt - Google Patents
A kind for the treatment of unit of abraum salt Download PDFInfo
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- CN204185249U CN204185249U CN201420666463.7U CN201420666463U CN204185249U CN 204185249 U CN204185249 U CN 204185249U CN 201420666463 U CN201420666463 U CN 201420666463U CN 204185249 U CN204185249 U CN 204185249U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The utility model discloses a kind for the treatment of unit of abraum salt, its structure comprises industrial feeder, multi-stage type indirect heater, Heat-conduction oil circulation system, the fused salt recycle system, organic exhaust gas transfer roller and abraum salt waste-heat recoverer.The feeding mouth of multi-stage type indirect heater is communicated with abraum salt waste-heat recoverer with industrial feeder respectively with discharge port; Multi-stage type indirect heater at least comprises first paragraph indirect heater and second segment indirect heater; First paragraph indirect heater connects with Heat-conduction oil circulation system, abraum salt waste-heat recoverer successively, and abraum salt waste-heat recoverer connects with first paragraph indirect heater and forms loop; Second segment indirect heater connects with the fused salt recycle system and forms loop; Organic exhaust gas transfer roller is arranged between the fused salt recycle system and multi-stage type indirect heater.The utility model effectively can complete the refining processing requirements of industrial waste salt, and solve exhaust gas emission problem, energy utilization efficiency is high simultaneously, and secondary pollution is few.
Description
Technical field
The utility model relates to a kind for the treatment of unit of waste, particularly relates to a kind for the treatment of unit of abraum salt.
Background technology
Industrial circle has a lot of enterprise to have abraum salt to produce, especially in field of fine chemical in process of production.As the production of pmida98, glyphosate, often produce 1 ton of glyphosate technicals, produce the useless sodium chloride salt containing various organic murder by poisoning thing of about 1.3 tons; As the production of AKD, often produce 1 ton of AKD, produces about 2 tons contain organic useless sodium chloride salt; As the production of hydrazine hydrate, often produce 1 ton of hydrazine hydrate, produce the useless sodium chloride salt of about 4 tons.These abraum salts, because of the restriction of production technique, are converted into solid waste by producer mostly, and owing to relating to large amount of organic composition in its production process, therefore this salt waste itself has certain toxicity.
At present, the process of abraum salt mainly adopts hot blast directly to contact high-temperature calcination method, utilizes the hot blast of a large amount of temperatures as high 600 ~ 800 DEG C directly to contact in calcining furnace with abraum salt, makes organism complete cracking process under the high temperature conditions.But this method due to abraum salt and hot blast limited for duration of contact, the temperature of salinity itself does not reach preferred temperature, and residual organic constituent content is restive.Meanwhile, because temperature is limited residing for organism, be difficult to permineralization, the organic constituent being converted into form more complicated greatly remains in hot blast.This in fact method is process solid contaminant transfer being become a kind of gaseous pollutant.
On the other hand, the equipment that can accept high-temperature process at present mainly contains rotary type process furnace, multi-layer discs pyrolyzer etc., these equipment mostly adopt high-temperature hot-air directly or indirectly and abraum salt carry out heat exchange operation, thus reach and allow abraum salt reach a high temperature to carry out the production of cracking, its treatment process efficiency is lower.For Pintsch process rotary type process furnace technique.Because burning adopts the mode of direct ignition burning, high-temperature tail gas temperature reaches 300 DEG C ~ 500 DEG C, directly outer row, and efficiency of combustion is less than 70%.
In addition, in fact will complete two processes, the first step completing heating pyrolyze, realize the drying of abraum salt, second step will realize the heating and calcining of salt.For the moisture abraum salt of 5%, the heat requirement supply of dry institute and calcining institute heat requirement supply as about 45%:55%.Both thermal loads are suitable, and prior art employing is single step operation, have ignored the thermal load requirement of material itself, is difficult to the design concept meeting less energy-consumption.After completing heating, material self-temperature is higher, in order to ensure the conveying under normal temperature condition, also needing to increase cooling apparatus, such as adopting water-cooled or air-cooled heat-exchange equipment.Therefore, supply from the heat of heat demand needed for the heating pyrolyze finally completing salt and actual consumption thermal source, the thermo-efficiency of current overall abraum salt treatment process is still less than 30%.
Utility model content
Because the above-mentioned defect of prior art, technical problem to be solved in the utility model is to provide a kind for the treatment of unit polluting little, that energy consumption is low, thermo-efficiency is high abraum salt.
For achieving the above object, the utility model provides a kind for the treatment of unit of abraum salt, comprises industrial feeder, multi-stage type indirect heater, Heat-conduction oil circulation system, the fused salt recycle system, organic exhaust gas transfer roller and abraum salt waste-heat recoverer; Described multi-stage type indirect heater has feeding mouth and discharge port, and described feeding mouth is communicated with described industrial feeder, and described discharge port is communicated with described abraum salt waste-heat recoverer; Described multi-stage type indirect heater at least comprises first paragraph indirect heater and second segment indirect heater, and described first paragraph indirect heater take thermal oil as heat source, described second segment indirect heater with liquid molten salt for heat source; Described first paragraph indirect heater connects with described Heat-conduction oil circulation system, described abraum salt waste-heat recoverer successively, and described abraum salt waste-heat recoverer connects with described first paragraph indirect heater and forms loop; Described second segment indirect heater connects with the described fused salt recycle system and forms loop; Described organic exhaust gas transfer roller is arranged between the described fused salt recycle system and described multi-stage type indirect heater, is delivered to the described fused salt recycle system for the waste gas produced by described multi-stage type indirect heater.
Further, described Heat-conduction oil circulation system comprises Heat-transfer Oil Pump, hot blast waste-heat recoverer, thermal oil storage tank, thermal oil circulation line and expansion slot, described Heat-transfer Oil Pump, to be communicated with by described thermal oil circulation line between described thermal oil storage tank and described hot blast waste-heat recoverer, described thermal oil storage tank is connected with described abraum salt waste-heat recoverer, and described hot blast waste-heat recoverer is connected with described first paragraph indirect heater by described expansion slot; Thermal oil can under the driving of described Heat-transfer Oil Pump, described abraum salt waste-heat recoverer is entered from described thermal oil storage tank, then described hot blast waste-heat recoverer, described expansion slot is entered successively, finally enter described first paragraph indirect heater, described thermal oil can be back to described heat conduction oil storage vessel in described first paragraph indirect heater with after abraum salt heat exchange.
Further, described thermal oil in described first paragraph indirect heater with the drying process that the heat transfer process of abraum salt is described abraum salt.
Further, the described fused salt recycle system comprises electrothermic type fused salt storage tank, pump for liquid salts, molten salt furnace, fused salt circulation line, described electrothermic type fused salt storage tank, described pump for liquid salts is communicated with by described fused salt circulation line with described molten salt furnace, described molten salt furnace is connected with described second segment indirect heater, hot melt salt liquefy melting salt after heating and melting in described electrothermic type fused salt storage tank, described liquid molten salt enters described molten salt furnace under the driving of described pump for liquid salts, and after being heated in described molten salt furnace, enter described second segment indirect heater, described liquid molten salt can be back to described electrothermic type fused salt storage tank in described second segment indirect heater with after abraum salt heat exchange.
Further, described liquid molten salt in described second segment indirect heater with the calcination process that the heat transfer process of abraum salt is described abraum salt.
Further, the described fused salt recycle system also comprises combustion engine and blower fan, described combustion engine is connected with described organic exhaust gas transfer roller, the organic tail gas produced in described multi-stage type indirect heater can be delivered to described combustion engine by described organic exhaust gas transfer roller, described organic tail gas burns in described combustion engine together with fuel, form combustion flame and be converted into inorganic component, described combustion flame is to the spiral heating coil pipe heating in described molten salt furnace, and the hot blast in described molten salt furnace and described combustion engine can be delivered to described hot blast waste-heat recoverer by described blower fan.
Further, described first paragraph indirect heater has dryer section well heater, and described dryer section well heater is used for abraum salt dry; Described Heat-conduction oil circulation system is to the delivered inside thermal oil of described dryer section well heater, and outside and the abraum salt of described dryer section well heater carry out contact heat-exchanging, thus makes abraum salt dry.
Further, described dryer section well heater is spiral pipe well heater or hollow disc well heater.
Further, described second segment indirect heater has heating zone well heater, and described heating zone well heater is used for heating abraum salt and calcining; The described fused salt recycle system is to the delivered inside liquid molten salt of described heating zone well heater, and outside and the abraum salt of described heating zone well heater carry out contact heat-exchanging.
Further, described heating zone well heater is spiral pipe well heater or hollow disc well heater.
Further, the inside of described abraum salt waste-heat recoverer has hollow vertical heat exchanging plate, and abraum salt can decline naturally along described hollow vertical heat exchanging plate; Described abraum salt waste-heat recoverer also has interlayer, and thermal oil can in described folder intrastratal flowage; Described abraum salt transfers heat to described thermal oil in decline process, thus completes heat transfer process.
Further, described abraum salt waste-heat recoverer is powder flow interchanger.
Further, described molten salt furnace adopts industrial combustion gas stove or industrial coal stove, and the inside of described molten salt furnace is provided with spiral heating coil pipe, and liquid fused salt sends described molten salt furnace after being heated in described spiral heating coil pipe.
Further, described hot blast waste-heat recoverer is gas liquid exchanger.
Further, described hot blast waste-heat recoverer is plate-type heat exchanger, plate-fin heat exchanger, shell-and-plate(heat)exchanger or tube and shell heat exchanger.
Further, described thermal oil is synthesis type thermal oil, and described synthesis type thermal oil is alkyl benzene-type (benzenoid form) thermal oil, alkylnaphthalene type thermal oil, alkyl biphenyl type thermal oil, biphenyl and Biphenyl Ether eutectic mixture type thermal oil or alkyl biphenyl ether type thermal oil.
Further, described melting salt adopts binary inorganic salt system or ternary inorganic salt system.
Further, described ternary inorganic salt system is 53Wt%KNO
3, 40Wt%NaNO
2and 7Wt%NaNO
3combined system, described binary inorganic salt system is 60Wt%NaNO
3and 40Wt%KNO
3combined system.
The technological process of the treatment unit of abraum salt of the present utility model comprises following four aspects:
(1) process of abraum salt: abraum salt is delivered to described first indirect heater by described industrial feeder, described abraum salt is in described first indirect heater after drying, under the effect of material-conveying mechanism, enter described second indirect heater, and in described second indirect heater, complete the process of heating and calcining; Salt after calcining enters described abraum salt waste-heat recoverer, and naturally decline in described abraum salt waste-heat recoverer, transfer heat to the thermal oil in described abraum salt waste-heat recoverer interlayer simultaneously, last described salt exports from abraum salt waste-heat recoverer, become discharging salt, described discharging salt is acceptable industrial salt.
(2) thermal oil working medium circulation: described Heat-conduction oil circulation system comprises Heat-transfer Oil Pump, hot blast waste-heat recoverer, thermal oil storage tank and expansion slot, thermal oil is under the driving of described Heat-transfer Oil Pump, described abraum salt waste-heat recoverer is entered from described thermal oil storage tank, then described hot blast waste-heat recoverer, described expansion slot is entered successively, finally enter described first paragraph indirect heater, described thermal oil is back to described thermal oil storage tank in described first paragraph indirect heater with after abraum salt heat exchange.
(3) hot melt salt working medium circulation: the described fused salt recycle system comprises electrothermic type fused salt storage tank, pump for liquid salts, molten salt furnace, hot melt salt liquefy melting salt after heating and melting in described electrothermic type fused salt storage tank, described liquid molten salt enters described molten salt furnace under the driving of described pump for liquid salts, and after being heated in described molten salt furnace, entering described second segment indirect heater, described liquid molten salt is back to described electrothermic type fused salt storage tank in described second segment indirect heater with after abraum salt heat exchange.
(4) process of hot blast and tail gas: the described fused salt recycle system also comprises combustion engine and blower fan, the organic tail gas produced in described multi-stage type indirect heater is delivered to described combustion engine through described organic exhaust gas transfer roller, described organic tail gas burns together with fuel with air mixed in the described combustion engine, form combustion flame, volatile organic matter under the high temperature hyperoxic conditions of described combustion engine in described organic tail gas burns and is converted into inorganic component, described combustion flame is to the spiral heating coil pipe heating in described molten salt furnace, hot blast in hot blast in described molten salt furnace and described combustion engine is delivered to described hot blast waste-heat recoverer by described blower fan, described hot blast in described hot blast waste-heat recoverer after heat exchange temperature be down to 80 ~ 200 DEG C, then through smoke stack emission to air.
Further, in described thermal oil working medium circulation, the temperature range of described thermal oil is 120 DEG C ~ 200 DEG C.
Further, in described hot melt salt working medium circulation, the temperature range of described liquid molten salt is 300 DEG C ~ 500 DEG C.
The beneficial effect of the treatment unit of abraum salt of the present utility model is:
The utility model adopts thermal oil working medium circulation and hot melt salt working medium circulation to carry out drying and calcination process to abraum salt respectively, greatly improves the efficiency of utilization of system.High temperature heat source needed in calcination process adopts melting salt, and the heat part that melting salt transmits is used for the organism thermo-cracking in abraum salt, and a part is recovered utilization and meets needed for the drying of charging abraum salt.The high-temperature hot-air produced in molten salt furnace and roasting kiln also realizes waste heat recovery by the heat trnasfer of thermal oil.The heat rejection produced in the treatment unit process abraum salt process of final abraum salt of the present utility model is only thermosteresis, the sensible heat of industrial qualified salt, the sensible heat of remaining tail gas of equipment, therefore overall thermal efficiency can reach 60 ~ 80%, improves 150% ~ 200% compared with traditional production technique thermo-efficiency.
Be described further below with reference to the technique effect of accompanying drawing to design of the present utility model, concrete structure and generation, to understand the purpose of this utility model, characteristic sum effect fully.
Accompanying drawing explanation
Fig. 1 is structural representation and the energy system figure of the treatment unit of the abraum salt of a preferred embodiment of the present utility model;
Fig. 2 is the schematic diagram of Heat-conduction oil circulation system in a preferred embodiment of the present utility model;
Fig. 3 is the schematic diagram of the fused salt recycle system in a preferred embodiment of the present utility model.
Embodiment
As shown in Figures 1 to 3, a preferred embodiment of the present utility model provides a kind for the treatment of unit of abraum salt, and its structure comprises industrial feeder 101, multi-stage type indirect heater, Heat-conduction oil circulation system, the fused salt recycle system, organic exhaust gas transfer roller 107 and abraum salt waste-heat recoverer 106; The feeding mouth of multi-stage type indirect heater is communicated with described industrial feeder 101, and its discharge port is communicated with abraum salt waste-heat recoverer 106; Multi-stage type indirect heater at least comprises first paragraph indirect heater 102 and second segment indirect heater 103, and first paragraph indirect heater 102 take thermal oil as heat source, second segment indirect heater 103 with liquid molten salt for heat source; First paragraph indirect heater 102 connects with the hot blast waste-heat recoverer 104 in Heat-conduction oil circulation system, abraum salt waste-heat recoverer 106 successively, and abraum salt waste-heat recoverer 106 connects with first paragraph indirect heater 102 and forms loop; Second segment indirect heater 103 connects with the molten salt furnace 105 in the fused salt recycle system and forms loop; Organic exhaust gas transfer roller 107 is arranged between combustion engine 110 in the fused salt recycle system and multi-stage type indirect heater, is delivered to combustion engine 110 for the tail gas that produced by multi-stage type indirect heater and waste gas.Arrow 108 in Fig. 1 is the transmission direction of thermal oil, and the direction of arrow 109 is the transmission direction of liquid molten salt.
In preferred embodiment of the present utility model, as shown in Figure 2, Heat-conduction oil circulation system comprises Heat-transfer Oil Pump 111, hot blast waste-heat recoverer 104, thermal oil storage tank 112, thermal oil circulation line 113 and expansion slot 114, Heat-transfer Oil Pump 111, to be communicated with by thermal oil circulation line 113 between thermal oil storage tank 112 and hot blast waste-heat recoverer 104, thermal oil storage tank 112 is connected with abraum salt waste-heat recoverer 106, and hot blast waste-heat recoverer 104 is connected with first paragraph indirect heater 102 by expansion slot 114; Thermal oil can under the driving of Heat-transfer Oil Pump 111, abraum salt waste-heat recoverer 106 is entered from thermal oil storage tank 112, then hot blast waste-heat recoverer 104, expansion slot 114 is entered successively, finally enter first paragraph indirect heater 102, thermal oil is back to heat conduction oil storage vessel 112 in first paragraph indirect heater 102 with after abraum salt heat exchange.Thermal oil is actual with the heat transfer process of abraum salt in first paragraph indirect heater 102 is the drying process of carrying out abraum salt.
The drying of first paragraph indirect heater 102 pairs of abraum salts is realized by the dryer section well heater of its inside, Heat-conduction oil circulation system is to the delivered inside thermal oil of dryer section well heater, the outside of dryer section well heater contacts with abraum salt, abraum salt indirectly with thermal oil heat exchange, thus make abraum salt dry.In the present embodiment, dryer section well heater is hollow disc well heater, also can be spiral pipe well heater in other embodiments.
As shown in Figure 3, the fused salt recycle system comprises electrothermic type fused salt storage tank 115, pump for liquid salts 116, molten salt furnace 105, fused salt circulation line 118, combustion engine 110 and blower fan 119.Wherein, electrothermic type fused salt storage tank 115, pump for liquid salts 116 are communicated with by fused salt circulation line 118 with molten salt furnace 105, molten salt furnace 105 is connected with second segment indirect heater 103, hot melt salt liquefy melting salt after heating and melting in electrothermic type fused salt storage tank 115, liquid molten salt enters molten salt furnace 105 under the driving of pump for liquid salts 116, and entering second segment indirect heater 103 after being heated in molten salt furnace 105, liquid molten salt is back to electrothermic type fused salt storage tank 115 in second segment indirect heater 103 with after abraum salt heat exchange.Liquid molten salt in second segment indirect heater 103 with the heat transfer process of abraum salt actual heating for carrying out dried abraum salt and calcination process.
The heating of second segment indirect heater 103 pairs of abraum salts and calcining are realized by the heating zone well heater of its inside, the fused salt recycle system is to the delivered inside liquid molten salt of heating zone well heater, the outside of heating zone well heater contacts with abraum salt, abraum salt indirectly with the heat exchange of liquid molten salt, thus abraum salt is calcined.In the present embodiment, heating zone well heater is hollow disc well heater, also can be spiral pipe well heater in other embodiments.
Combustion engine 110 is connected with organic exhaust gas transfer roller 107, and organic exhaust gas transfer roller 107 arrow 120 organic tail gas produced in multi-stage type indirect heater can be delivered in combustion engine 110, Fig. 3 be the flow direction of organic tail gas.Organic tail gas burns in combustion engine 110 together with fuel, forms combustion flame and is converted into inorganic component, and combustion flame is to the spiral heating coil pipe heating in molten salt furnace 105.Hot blast in molten salt furnace 105 and combustion engine 110 can be delivered to hot blast waste-heat recoverer 104 by blower fan 119.
In preferred embodiment of the present utility model, abraum salt waste-heat recoverer 106 is powder flow interchanger, and its inside has hollow vertical heat exchanging plate, and abraum salt can decline naturally along this hollow vertical heat exchanging plate; Abraum salt waste-heat recoverer 106 also has interlayer, and thermal oil can in this folder intrastratal flowage.Abraum salt transfers heat to thermal oil in decline process, thus completes heat transfer process.
In preferred embodiment of the present utility model, the inside of molten salt furnace 105 is provided with spiral heating coil pipe, and liquid fused salt sends described molten salt furnace after being heated in spiral heating coil pipe.Molten salt furnace 105 adopts industrial combustion gas stove, also can adopt industrial coal stove in other embodiments,
Hot blast waste-heat recoverer 104 is gas liquid exchanger, adopts plate-type heat exchanger in the present embodiment, can be plate-fin heat exchanger, shell-and-plate(heat)exchanger in other embodiments, or tube and shell heat exchanger.
Thermal oil is synthesis type thermal oil, such as alkyl benzene-type (benzenoid form) thermal oil, alkylnaphthalene type thermal oil, alkyl biphenyl type thermal oil, biphenyl and Biphenyl Ether eutectic mixture type thermal oil or alkyl biphenyl ether type thermal oil.
In preferred embodiment of the present utility model, melting salt adopts ternary inorganic salt 53Wt%KNO
3, 40Wt%NaNO
2and 7Wt%NaNO
3combined system, also can adopt binary inorganic salt 60Wt%NaNO in other embodiments
3and 40Wt%KNO
3combined system.
The technological process of the treatment unit of the abraum salt of the present embodiment comprises following four aspects:
(1) process of abraum salt: abraum salt is delivered to the first indirect heater 102 by industrial feeder 101, abraum salt is in the first indirect heater 102 after drying, under the effect of material-conveying mechanism, enter the second indirect heater 103, and in the second indirect heater 103, complete the process of heating and calcining; Salt after calcining enters abraum salt waste-heat recoverer 106, and naturally decline in abraum salt waste-heat recoverer 106, transfer heat to the thermal oil in the interlayer of abraum salt waste-heat recoverer 106 simultaneously, finally export from abraum salt waste-heat recoverer 106, become discharging salt, this discharging salt is acceptable industrial salt.
(2) thermal oil working medium circulation: thermal oil is under the driving of Heat-transfer Oil Pump 111, abraum salt waste-heat recoverer 106 is entered from thermal oil storage tank 112, then hot blast waste-heat recoverer 104, expansion slot 114 is entered successively, finally enter first paragraph indirect heater 102, thermal oil is back to thermal oil storage tank 112 in first paragraph indirect heater 102 with after abraum salt heat exchange.
(3) hot melt salt working medium circulation: hot melt salt liquefy melting salt after heating and melting in electrothermic type fused salt storage tank 115, liquid molten salt enters molten salt furnace 105 under the driving of pump for liquid salts 116, and entering second segment indirect heater 103 after being heated in molten salt furnace 105, liquid molten salt is back to electrothermic type fused salt storage tank 115 in second segment indirect heater 103 with after abraum salt heat exchange.
(4) process of hot blast and tail gas: the organic tail gas produced in multi-stage type indirect heater is delivered to combustion engine 110 through organic exhaust gas transfer roller 107, then organic tail gas in combustion engine 110 with air mixed, and burn together with fuel, form combustion flame.The temperature of combustion flame is more than 1100 DEG C, and the volatile organic matter burning at this temperature in organic tail gas can realize permineralization and be converted into inorganic component, thus achieves harmless treatment.Combustion flame is also to the spiral heating coil pipe heating in molten salt furnace 105.Hot blast in hot blast in molten salt furnace 105 and combustion engine 110 is delivered to hot blast waste-heat recoverer 104 by blower fan 119, hot blast in hot blast waste-heat recoverer 104 after heat exchange temperature be down to 80 ~ 200 DEG C, then through smoke stack emission to air.
Fig. 1 gives the energy system figure of the treatment unit of the abraum salt of preferred embodiment of the present utility model, and the combustion air of assumptions' environment temperature and abraum salt heat are zero, then the present embodiment process heat load meets following balance:
Q1+Q5+Q7＝Q2+Q3+ΔQ1
Q3+Q8=Q4+Q
row+ Δ Q2
Q2+Q4＝Q5+Q6+Q7+Q9+ΔQ3
Q9+Q6＝Q8+Q10+ΔQ4
Q1=Δ Q1+ Δ Q2+ Δ Q3+ Δ Q4+Q
row+ Q10
Wherein, Q1 is fuel combustion supply heat; Q2 exports liquid fused salt institute heat content for molten salt furnace 105; Q3 is molten salt furnace 105 combustion tail gas institute heat content; Q4 exports institute's heat content at hot blast waste-heat recoverer 104 for thermal oil; Q5 is institute's heat content in multi-stage type indirect heater generation organic exhaust gas; Q6 is for thermal oil is in first paragraph indirect heater 102 exit institute heat content; Q7 is for thermal oil is in second segment indirect heater 103 exit institute heat content; Q8 is for thermal oil is in abraum salt waste-heat recoverer 106 exit institute heat content; Q9 exports hot salt institute heat content for second segment indirect heater 103; Q10 is abraum salt waste-heat recoverer 106 exit industry qualified salt institute heat content; Δ Q1 is the thermosteresis of molten salt furnace 105 and auxiliary member; Δ Q2 is the thermosteresis of hot blast waste-heat recoverer 104 and auxiliary member; Δ Q3 is the thermosteresis of multi-zone reheating furnace and auxiliary member; Δ Q4 is the thermosteresis of abraum salt waste-heat recoverer 106 and auxiliary member.
For certain factory hydrazine hydrate evaporative crystallization abraum salt 50kg/h, in this abraum salt, major ingredient is sodium chloride salt, and abraum salt contains total organic carbon 130mg/L (in saturated brine), water ratio 4% (Wt/Wt%).After the production technique of the present embodiment processes, qualified product salt sodium chloride content is 99.5% (Wt/Wt%), and in product salt, total organic carbon is 7mg/L (in saturated brine).
In the present embodiment, the dryer section in multi-stage type indirect heater, namely the thermal oil charging oil temperature of the first indirect heater 102 is 180 DEG C, and discharging oil temperature is 120 DEG C.Heating zone in multi-stage type indirect heater, namely the charging temperature of molten salt of the second indirect heater 103 is 450 DEG C, and discharging temperature of molten salt is 420 DEG C.
In multi-stage type indirect heater, abraum salt feeding temperature is 20 DEG C, and abraum salt drop temperature is 380 DEG C, and the drop temperature of abraum salt waste-heat recoverer 106 is 120 DEG C.
In implementation process, gas-firing consumption is 0.68Nm
3/ h, with calorific value 31MJ/Nm
3consider, burning input heat is 21.08MJ/h.Abraum salt treatment capacity is 50kg/h, and be warming up to 380 DEG C of heats completing the purified salt of heating with the salt completed dry at 80 DEG C and calculate, institute's heat requirement is 13.97MJ/h, and the overall thermal efficiency that can obtain the present embodiment is 66%.
More than describe preferred embodiment of the present utility model in detail.Should be appreciated that those of ordinary skill in the art just can make many modifications and variations according to design of the present utility model without the need to creative work.Therefore, all technician in the art according to design of the present utility model on the basis of existing technology by the available technical scheme of logical analysis, reasoning, or a limited experiment, all should by the determined protection domain of claims.
Claims (10)
1. a treatment unit for abraum salt, is characterized in that, comprises industrial feeder, multi-stage type indirect heater, Heat-conduction oil circulation system, the fused salt recycle system, organic exhaust gas transfer roller and abraum salt waste-heat recoverer; Wherein, described multi-stage type indirect heater has feeding mouth and discharge port, and described feeding mouth is communicated with described industrial feeder, and described discharge port is communicated with described abraum salt waste-heat recoverer; Described multi-stage type indirect heater at least comprises first paragraph indirect heater and second segment indirect heater; Described first paragraph indirect heater connects with described Heat-conduction oil circulation system, described abraum salt waste-heat recoverer successively, and described abraum salt waste-heat recoverer connects with described first paragraph indirect heater and forms loop; Described second segment indirect heater connects with the described fused salt recycle system and forms loop; Described organic exhaust gas transfer roller is arranged between the described fused salt recycle system and described multi-stage type indirect heater, is delivered to the described fused salt recycle system for the waste gas produced by described multi-stage type indirect heater.
2. the treatment unit of abraum salt as claimed in claim 1, it is characterized in that, described Heat-conduction oil circulation system comprises Heat-transfer Oil Pump, hot blast waste-heat recoverer, thermal oil storage tank, thermal oil circulation line and expansion slot, described Heat-transfer Oil Pump, to be communicated with by described thermal oil circulation line between described thermal oil storage tank and described hot blast waste-heat recoverer, described thermal oil storage tank is connected with described abraum salt waste-heat recoverer, and described hot blast waste-heat recoverer is connected with described first paragraph indirect heater by described expansion slot; Thermal oil can under the driving of described Heat-transfer Oil Pump, described abraum salt waste-heat recoverer is entered from described thermal oil storage tank, then described hot blast waste-heat recoverer, described expansion slot is entered successively, finally enter described first paragraph indirect heater, described thermal oil can be back to described heat conduction oil storage vessel in described first paragraph indirect heater with after abraum salt heat exchange.
3. the treatment unit of abraum salt as claimed in claim 1, it is characterized in that, described hot blast waste-heat recoverer is gas liquid exchanger.
4. the treatment unit of abraum salt as claimed in claim 1, it is characterized in that, the described fused salt recycle system comprises electrothermic type fused salt storage tank, pump for liquid salts, molten salt furnace, fused salt circulation line, described electrothermic type fused salt storage tank, described pump for liquid salts is communicated with by described fused salt circulation line with described molten salt furnace, described molten salt furnace is connected with described second segment indirect heater, hot melt salt liquefy melting salt after heating and melting in described electrothermic type fused salt storage tank, described liquid molten salt enters described molten salt furnace under the driving of described pump for liquid salts, and after being heated in described molten salt furnace, enter described second segment indirect heater, described liquid molten salt can be back to described electrothermic type fused salt storage tank in described second segment indirect heater with after abraum salt heat exchange.
5. the treatment unit of abraum salt as claimed in claim 4, it is characterized in that, described molten salt furnace adopts industrial combustion gas stove or industrial coal stove, and the inside of described molten salt furnace is provided with spiral heating coil pipe, and liquid fused salt sends described molten salt furnace after being heated in described spiral heating coil pipe.
6. the treatment unit of abraum salt as claimed in claim 4, it is characterized in that, the described fused salt recycle system also comprises combustion engine and blower fan, described combustion engine is connected with described organic exhaust gas transfer roller, the organic tail gas produced in described multi-stage type indirect heater can be delivered to described combustion engine by described organic exhaust gas transfer roller, described organic tail gas burns in described combustion engine together with fuel, form combustion flame and be converted into inorganic component, described combustion flame is to the spiral heating coil pipe heating in described molten salt furnace, hot blast in described molten salt furnace and described combustion engine can be delivered to described hot blast waste-heat recoverer by described blower fan.
7. the treatment unit of abraum salt as claimed in claim 1, it is characterized in that, described first paragraph indirect heater has dryer section well heater, and described dryer section well heater is used for abraum salt dry; Described Heat-conduction oil circulation system is to the delivered inside thermal oil of described dryer section well heater, and outside and the abraum salt of described dryer section well heater carry out contact heat-exchanging, thus makes abraum salt dry.
8. the treatment unit of abraum salt as claimed in claim 1, it is characterized in that, described second segment indirect heater has heating zone well heater, and described heating zone well heater is used for heating abraum salt and calcining; The described fused salt recycle system is to the delivered inside liquid molten salt of described heating zone well heater, and outside and the abraum salt of described heating zone well heater carry out contact heat-exchanging.
9. the treatment unit of abraum salt as claimed in claim 1, it is characterized in that, the inside of described abraum salt waste-heat recoverer has hollow vertical heat exchanging plate, and abraum salt can decline naturally along described hollow vertical heat exchanging plate; Described abraum salt waste-heat recoverer also has interlayer, and thermal oil can in described folder intrastratal flowage; Described abraum salt transfers heat to described thermal oil in decline process, thus completes heat transfer process.
10. the treatment unit of abraum salt as claimed in claim 1, it is characterized in that, described thermal oil is synthesis type thermal oil, and described melting salt adopts binary inorganic salt system or ternary inorganic salt system.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105439231A (en) * | 2015-12-22 | 2016-03-30 | 清华大学 | Method for processing coal-chemical-industry salt-containing sewage based in furnace internal combustion |
| CN106115303A (en) * | 2016-08-30 | 2016-11-16 | 安徽今朝环保科技有限公司 | Salt circulating industrial waste salt blanking device and using method thereof |
| WO2022267155A1 (en) * | 2021-06-23 | 2022-12-29 | 北京蓝海翌能新能源集团有限公司 | Solar photo-thermal power station salt melting system based on heat transfer oil heat collection field |
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2014
- 2014-11-10 CN CN201420666463.7U patent/CN204185249U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105439231A (en) * | 2015-12-22 | 2016-03-30 | 清华大学 | Method for processing coal-chemical-industry salt-containing sewage based in furnace internal combustion |
| CN105439231B (en) * | 2015-12-22 | 2018-01-16 | 清华大学 | Method based on burning processing coal chemical industry saline sewage in stove |
| CN106115303A (en) * | 2016-08-30 | 2016-11-16 | 安徽今朝环保科技有限公司 | Salt circulating industrial waste salt blanking device and using method thereof |
| WO2022267155A1 (en) * | 2021-06-23 | 2022-12-29 | 北京蓝海翌能新能源集团有限公司 | Solar photo-thermal power station salt melting system based on heat transfer oil heat collection field |
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