CN203754456U - Nitrogen circulation type low-temperature evaporation concentration device - Google Patents
Nitrogen circulation type low-temperature evaporation concentration device Download PDFInfo
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- CN203754456U CN203754456U CN201420150563.4U CN201420150563U CN203754456U CN 203754456 U CN203754456 U CN 203754456U CN 201420150563 U CN201420150563 U CN 201420150563U CN 203754456 U CN203754456 U CN 203754456U
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Abstract
The utility model discloses a nitrogen circulation type low-temperature evaporation concentration device which comprises a Carnot heating circulation device and an evaporation concentrator, wherein the Carnot heating circulation device comprises a compressor, an evaporator, an expansion valve and a condenser which are circularly connected through pipelines; a heating-side inlet of the condenser is connected with a feeding pipeline; an air circulation channel is formed in the evaporation concentrator and comprises a feed liquid concentration region and a condensed water generation region, and a fan for blowing cold air in the condensed water generation region to the feed liquid concentration region is arranged at the bottom of the air circulation channel; and at least one oxygen remover supply device is arranged on a pipeline of the device. The device has the beneficial effects that the oxygen absorption corrosion is remarkably reduced; the desalting, the dewatering and/or the recovery of high-concentration salt and highly polluted wastewater are carried out at a low temperature (40-95 DEG C) under normal pressure, and byproducts-clean condensed water can be produced; and the purpose of zero discharge is achieved.
Description
Technical field
The utility model relates to field of waste water treatment, particularly a kind of low-temperature evaporation concentration device of nitrogen circulation.
Background technology
The bittern of high density and chemical wastewater can not directly enter municipal wastewater system, the mode of processing: the 1st kind of mode is to transport special factory processes to, because expense is higher, these waste water can only store on the spot, until there is no storage space.The 2nd kind of mode is that to carry out multiple-effect evaporation into multiple-effect evaporator concentrated, but must have steam supply, and the progression of multiple-effect evaporator 3 to 6 o'clock, efficiency could be higher, and for backward feed flow process, the outflow temperature that completes liquid is higher, also further flash concentration, further improves efficiency.The 3rd kind of mode is to enter crystallizer into mechanically compress recirculation system (being MVR vaporizer) and reconcentration liquid subsequently to carry out crystallization, use again equipment for separating liquid from solid fractional crystallization thing, the efficiency of this MVR vaporizer is very high, but under middle low temperature condition, during due to middle low temperature, saturation vapor pressure is lower, need to go compression with respect to (100kPa steam entry pressure) with large several-fold vapour compressor, because saturation vapor pressure 70.1 kPa at 90 DEG C; 80 DEG C--47.3 kPa; 70 DEG C--31.2 kPa; 60 DEG C--19.9 kPa; 50 DEG C--12.3 kPa; 40 DEG C--7.4kPa, cost increases more.The 4th kind of mode is to adopt low-temperature evaporation concentration device, its principle is that cold medium heat pump technology is in conjunction with reclaiming the water vapour latent heat of feed liquid to the technology of low temperature feed liquid, this technology the applicant has applied for Chinese utility model patent (application number 201320719866.9) and patent of invention (application number 2013105682572) simultaneously, the 2nd kind of which energy loss-rate is low, under middle low temperature condition a little more than the 3rd kind of mode, but equipment cost is lower than the 2nd mode.Even so, but because the non-condensable gases in recycle gas is air, easily cause interchanger oxygen uptake corrosion under comparatively high temps and humidity, the interchanger life-span is shorter.
Utility model content
For the problems referred to above, the purpose of this utility model is to provide a kind of can effectively eliminate the oxygen in the recycle gas in low-temperature evaporation concentration device, and can carry out at low temperatures the low-temperature evaporation concentration device of the nitrogen circulation of the nitrogen circulation of high power evaporation concentration.
For achieving the above object, the technical scheme that the utility model proposes is: a kind of low-temperature evaporation concentration device of nitrogen circulation, it is characterized in that: comprise that Kano heats circulation device, an evaporation concentrator, described Kano heat circulation device comprise by pipeline circulate connect compressor, vaporizer, expansion valve, condenser; Described condenser heat absorbing side import connects feed pipe;
In described evaporation concentrator, be provided with an air circulation duct, air circulation duct comprises that a feed liquid enrichment region and a water of condensation generate district, and air circulation duct bottom is provided with one water of condensation is generated to freezing air in district and blow to the blower fan of feed liquid enrichment region;
Described feed liquid enrichment region is provided with a gas-liquid heat exchange device that carries out heat exchange for hot feed liquid and freezing air, and gas-liquid heat exchange device is connected with the heat absorbing side outlet of condenser; Below, feed liquid enrichment region is provided with a taper feed liquid collection unit;
Described water of condensation generates district and is provided with First Heat Exchanger, in feed liquid enrichment region, blow over the warm air coming and connect First Heat Exchanger heat release side entrance, the heat absorbing side outlet of First Heat Exchanger is connected with feed pipe by pipeline, water of condensation generates below, district and is provided with a taper condensation water collection portion, and taper condensation water collection portion is connected with condensation water collection tank by pipeline;
Also comprise the second interchanger, the heat absorbing side import of the second interchanger is connected refrigerant outlet and the refrigerant inlet of refrigeration agent generating apparatus with heat absorbing side outlet; The second described interchanger is located in evaporation concentrator or is located at outside evaporation concentrator;
In the time that the second described interchanger is located in evaporation concentrator: described taper feed liquid collection unit connects the heat absorbing side import of First Heat Exchanger by pipeline, the first material pump, the heat release side outlet of First Heat Exchanger connects the heat release side-entrance of the second interchanger, and the freezing air of the heat release side outlet of the second interchanger blows to blower fan;
In the time that the second described interchanger is located at evaporation concentrator outside: described taper feed liquid collection unit connects the heat release side-entrance of the second interchanger by pipeline, the first material pump, the heat release side outlet of the second interchanger connects the heat absorbing side import of First Heat Exchanger, and the freezing air of the heat release side outlet of First Heat Exchanger blows to blower fan;
On the pipeline of the low-temperature evaporation concentration device of described nitrogen circulation, be at least provided with an oxygen scavenger feedway.
Preferably, described oxygen scavenger feedway comprises the oxygen scavenger hold-up vessel connected by transport pipe, oxygen scavenger transferpump, and described transport pipe is connected with the pipeline of low-temperature evaporation concentration device.
Preferably, described oxygen scavenger feedway is located on ducted one or more positions of pipeline between feed pipe, taper feed liquid collection unit and the first material pump, the second interchanger heat absorbing side import.
Preferably, in described oxygen scavenger hold-up vessel, stored oxygen scavenger is preferably 10% sodium sulfite solution or 10% sodium sulfite solution.
Preferably, also comprise an indirect heat exchanger, the heat absorbing side import of described indirect heat exchanger connects feed pipe, and the heat release side-entrance of indirect heat exchanger, heat release side outlet are connected with heat absorbing side outlet, heat absorbing side import that Kano heats in the condenser of circulation device respectively; Described gas-liquid heat exchange device is connected with the outlet of the heat absorbing side of indirect heat exchanger.
Further, described gas-liquid heat exchange device is spray thrower or cooling tower without draught fan.
Preferably, the air circulation duct of described gas-liquid heat exchange device top is provided with a demist plate.
Further, on described feed pipe, being also provided with a shunt conduit is connected with taper feed liquid collection unit.
Further, in the time that the second interchanger is located in evaporation concentrator, also comprise the first equipment for separating liquid from solid, the first described material pump discharge is connected with the first outlet with the entrance of the first equipment for separating liquid from solid respectively with the import of First Heat Exchanger heat absorbing side; In the time that the second interchanger is located at outside evaporation concentrator, also comprise the first equipment for separating liquid from solid and the second equipment for separating liquid from solid, the first described material pump discharge is connected with the first outlet with the entrance of the first equipment for separating liquid from solid respectively with the second interchanger heat release side entrance, and the second described interchanger heat release side outlet is connected with the first outlet with the second equipment for separating liquid from solid entrance respectively with the import of First Heat Exchanger heat absorbing side.
Concrete, on the first equipment for separating liquid from solid and the second equipment for separating liquid from solid, all comprise entrance, the first outlet and the second outlet, entrance is to be connected with the pipeline that contains the supersaturated solution of separating out solid (as grease or crystal etc.) that flows, the first outlet is connected with the pipeline that does not contain or contain less the supersaturated solution of separating out solid (as grease or crystal etc.) that flows, second export be connected with the mobile pipeline that contains more supersaturated solution of separating out solid (as grease or crystal etc.) or with contain moist solids pipeline and be connected; Its effect is to utilize centrifugal force or membrane filtration technique means to be divided into 2 plumes by containing the supersaturated solution of crossing of separating out solid: a plume is not contain or contain less the supersaturated solution of separating out solid (as grease or crystal etc.), and another plume is to be connected or to be connected with the material mouth that contains moist solids with the pipeline that contains more supersaturated solution of separating out solid (as grease or crystal etc.) that flows.
Further, described taper feed liquid collection unit is biconical feed liquid collection unit, biconical feed liquid collection unit comprises the first taper feed liquid collection unit and the second taper feed liquid collection unit, the first taper feed liquid collection unit is provided with a filtering net, and the first taper feed liquid collection unit is connected with the heat absorbing side import of First Heat Exchanger by pipeline, the first material pump; The second taper feed liquid collection unit connects the entrance of the first equipment for separating liquid from solid by the second material pump, the first outlet of the first equipment for separating liquid from solid connects the first taper feed liquid collection unit.
Further, described refrigeration agent generating apparatus is that Kano heats circulation device, and the heat absorbing side outlet of the second interchanger connects the pipeline between compressor and vaporizer, and the heat absorbing side import of the second interchanger connects the pipeline between vaporizer and expansion valve; Or the heat absorbing side import of the second interchanger connects the pipeline between compressor and vaporizer, the heat absorbing side outlet of the second interchanger connects the pipeline between vaporizer and expansion valve.
Further, in the time being provided with indirect heat exchanger, also comprise an expansion tank, recycle pump, described expansion tank water outlet is connected with recycle pump, the import of condenser heat absorbing side by pipeline, the outlet of condenser heat absorbing side is connected with indirect heat exchanger heat release side-entrance by pipeline, and indirect heat exchanger heat release side outlet connects the pipeline between expansion tank water-in or expansion tank and recycle pump.
Preferably, the refrigeration agent that described Kano heats in circulation device is preferably R717.
Adopt technique scheme, the low-temperature evaporation concentration device of nitrogen circulation described in the utility model, the beneficial effect having is:
1) significantly reduce oxygen uptake corrosion;
2) less energy-consumption realizes deoxygenation object: can be low to moderate 0.1 degree electricity/ton waste water (containing the dynamic power of oxygen scavenger pump and institute's consuming electric power of evaporation oxygen scavenger solution);
3) desalination under low temperature (40 DEG C-95 DEG C) normal pressure, dehydration and (or) recovery high salt concentration and highly polluted waste water;
4) because dripping feed liquid just separates out a small amount of solid at every turn, cause salification, fouling chance to greatly reduce, so only need a small amount of cleaning;
5) low-temperature evaporation is more suitable for the feed liquid processing of heat sensitivity;
6) can produce the water of condensation that byproduct is clean;
7) zero release;
8), for high salt concentration waste water, waste water from dyestuff and oil wastewater, reclaim high salt concentration or dyestuff or grease.
Brief description of the drawings
Fig. 1 is that low-temperature evaporation concentration device is not installed oxygen scavenger feedway schematic diagram 1;
Fig. 2 is that low-temperature evaporation concentration device is not installed oxygen scavenger feedway schematic diagram 2;
Fig. 3 is that low-temperature evaporation concentration device is not installed oxygen scavenger feedway schematic diagram 3;
Fig. 4 is that low-temperature evaporation concentration device is not installed oxygen scavenger feedway schematic diagram 4;
Fig. 5 is that low-temperature evaporation concentration device is not installed oxygen scavenger feedway schematic diagram 5;
Fig. 6 is installation oxygen scavenger feedway low-temperature evaporation concentration device schematic diagram described in the utility model;
Fig. 7 is oxygen scavenger feedway structural representation.
Embodiment
Below in conjunction with the drawings and specific embodiments, the utility model is described further.
As Figure 1-Figure 5, amount to the low-temperature evaporation concentration device schematic diagram of the nitrogen circulation of device for deoxygenation is not installed, this part the applicant earlier application patent, but because patent is also unexposed, in this openly explanation in the lump.
As shown in Figure 1, nitrogen circulation low-temperature evaporation concentration device, comprise that Kano heats circulation device 1, an evaporation concentrator 3, described Kano heat circulation device 1 comprise by pipeline circulate connect compressor 101, vaporizer 102, expansion valve 103, condenser 104; The heat absorbing side import of condenser 104 connects feed pipe 4; In described evaporation concentrator 3, be provided with an air circulation duct 31, air circulation duct 31 comprises that a feed liquid enrichment region 311 and a water of condensation generate district 312, and air circulation duct 31 bottoms are provided with one water of condensation is generated to freezing air in district 312 and blow to the blower fan 32 of feed liquid enrichment region 311;
Described water of condensation generates district 312 and is provided with First Heat Exchanger 7, the second interchanger 8, in feed liquid enrichment region 311, blow over the warm air coming and connect First Heat Exchanger 7 heat release side entrances, the heat release side outlet of First Heat Exchanger 7 connects the heat release side-entrance of the second interchanger 8, the freezing air of the heat release side outlet of the second interchanger 8 blows to blower fan 32, the heat absorbing side import of the second interchanger 8 is connected refrigerant outlet and the refrigerant inlet of refrigeration agent generating apparatus 9 with heat absorbing side outlet, water of condensation generates 312 belows, district and is provided with a taper condensation water collection portion 10, taper condensation water collection portion 10 is connected with condensation water collection tank 11 by pipeline,
Described feed liquid enrichment region 311 is provided with a gas-liquid heat exchange device 12 that carries out heat exchange for hot feed liquid and freezing air, and in the present embodiment, gas-liquid heat exchange device 12 is spray thrower; Also can be cooling tower without draught fan.Gas-liquid heat exchange device 12 tops are preferably provided with a demist plate 20.Gas-liquid heat exchange device 12 is connected with the heat absorbing side outlet of condenser 104; 311 belows, feed liquid enrichment region are provided with a taper feed liquid collection unit 13, taper feed liquid collection unit 13 connects the heat absorbing side import of the first equipment for separating liquid from solid 15 entrances 150, the first equipment for separating liquid from solid 15 first outlet 151 connection First Heat Exchangers 7 by pipeline, the first material pump 14, the second outlet 152 of the first equipment for separating liquid from solid 15 is discharged and is contained more supersaturated solution of separating out solid (as grease or crystal etc.), and the heat absorbing side outlet of First Heat Exchanger 7 is connected with feed pipe 4 by pipeline; On feed pipe 4, being also provided with a shunt conduit 16 is connected with taper feed liquid collection unit 13.
As shown in Figure 2, the difference of itself and Fig. 1 is, also be provided with an indirect heat exchanger 2, the heat absorbing side import of indirect heat exchanger 2 connects feed pipe 4, also comprise an expansion tank 5, recycle pump 6, expansion tank 5 water outlets are connected with recycle pump 6, condenser 104 heat absorbing side imports by pipeline, condenser 104 heat absorbing side outlets are connected with indirect heat exchanger 2 heat release side-entrances by pipeline, and indirect heat exchanger 2 heat release side outlets connect expansion tank 5 water-ins also can be connected in the pipeline between expansion tank and recycle pump; Gas-liquid heat exchange device 12 is connected with the heat absorbing side outlet of indirect heat exchanger 2.
As shown in Figure 3, the difference of itself and Fig. 2 is: taper feed liquid collection unit 13 is biconical feed liquid collection unit, biconical feed liquid collection unit comprises the first taper feed liquid collection unit 131 and the second taper feed liquid collection unit 132, the first taper feed liquid collection unit 131 is provided with filtering net 17, the first taper feed liquid collection units and is connected with the heat absorbing side import of First Heat Exchanger 7 by pipeline, the first material pump 14; The first outlet 151 that the second taper feed liquid collection unit 132 connects the first equipment for separating liquid from solid 15 entrance 150, the first equipment for separating liquid from solid 15 by the second material pump 18 connects the first taper feed liquid collection unit 131.
As described in Figure 4: the difference of itself and Fig. 2 is: refrigeration agent generating apparatus 9 directly adopts Kano to heat circulation device 1, the heat absorbing side outlet of the second interchanger 8 connects the pipeline between compressor 101 and vaporizer 102, and the heat absorbing side import of the second interchanger 8 connects the pipeline between vaporizer 102 and expansion valve 103.
As shown in Figure 5, the difference of itself and Fig. 2 is, the second described interchanger 8 is located at evaporation concentrator 3 outsides, and taper feed liquid collection unit 13 is passed through pipeline, the first material pump 14, the first equipment for separating liquid from solid 15 first outlets 151 connect the heat release side-entrance of the second interchanger 8, the heat release side outlet of the second interchanger 8 connects the second equipment for separating liquid from solid 19 entrances 190, the second equipment for separating liquid from solid 19 first outlets 191 connect the heat absorbing side import of First Heat Exchanger 7, the second equipment for separating liquid from solid second exports 192 discharges and contains the more solid of separating out (as grease, or crystal etc.) supersaturated solution, the freezing air of the heat release side outlet of First Heat Exchanger 7 blows to blower fan 32, adopt the object of which to be, with the refrigeration agent feed liquid enrichment region cold burden liquid out of lowering the temperature, generate temperature lower cold burden liquid and enter again First Heat Exchanger to make to generate from water of condensation the air in district lower, thereby avoid the air themperature of air circulation duct to continue to rise.
When concrete use, taking the low-temperature evaporation concentration device of Fig. 2 as example, from vaporizer low-temp low-pressure gaseous coolant R717 out, at the gaseous coolant that becomes High Temperature High Pressure after compressor compresses, then through condenser, heat exchange discharges after heat of liquefaction, is condensed into the liquid refrigerants of High Temperature High Pressure; The liquid refrigerants of the liquid refrigerants of High Temperature High Pressure low-temp low-pressure after expansion valve, the liquid refrigerants of low-temp low-pressure absorbs heat and flashes to the gaseous coolant of low-temp low-pressure through wind-cooled evaporator.Liquid out from expansion tank, then after pump pressurization, flows to the condenser intensification of absorbing heat gradually, out becomes hot water, meanwhile at heat release side refrigerant by gaseous state liquefy.Flow to indirect heat exchanger from condenser hot water out, heat is passed to the mixed liquor of 2 bursts of different temperature difference, cooling gradually, gets back to expansion tank from the water coolant of indirect heat exchanger lesser temps out simultaneously;
From the waste water (bittern of high density and chemical wastewater) of technique discharge, i.e. high-concentration waste water, goes indirect heat exchanger heat absorption to heat up with from the higher waste water of First Heat Exchanger temperature out after mixing, become thermal wastewater;
Thermal wastewater by spray part evaporation and distribute heat to freezing air, thereby make freezing air become Hot wet air heating, thermal wastewater loss water vapour is concentrated, and after heat exchange, becomes cold waste water.Be collected in the cold waste water of bottom taper feed liquid collection unit, (because causing the solute concentration that solubleness reduces and evaporation causes, cooling rises, along with circulation is constantly carried out, solute concentration has risen to gradually solid and has separated out), first after solid-liquid separation by the first material pump, enter First Heat Exchanger, carry out counterflow heat exchange with the more Hot wet air heating of vapor volume content and absorb most of heat, make cold waste water heat absorption become the waste water that temperature is higher, and the higher waste water of temperature and raw material high-concentration waste water enter indirect heat exchanger after mixing and carry out heat exchange intensification, thereby reclaim most of Air Temperature Difference heat and steam latent heat.Carry out further cooling through the second interchanger again from First Heat Exchanger freezing air out and become compared with freezing air, and after pressurizeing by blower fan compared with freezing air, flow to feed liquid enrichment region; Wherein Hot wet air heating produces water of condensation and finally falls/flow to condensed water collecting device after the cooling of First Heat Exchanger and the second interchanger, and water of condensation in condensed water collecting device is pressurizeed and got by water pump.
Rough calculation is once: due to vapour latent heat: 2260KJ/Kg, directly become with electric-heating water the electric energy number of degrees=2260*1000*1000/3600/1000 ≈ 628 (degree) that one ton of steam need to consume; This system adopts Kano to heat circulation and reclaims the theoretical rough calculation value of vaporization heat and heat radiation:
Kano heats circulation: 30 DEG C of sink temperatures, 85 DEG C of heat source temperatures, so R717 refrigerant heat circulation COP< (273+85)/((273+85)-(273+30))=6.51, obtain the enthalpy about 1480KJ/Kg of R717 at 30 DEG C of low-temp low-pressure gaseous states and look into R717 refrigerant pressure-enthalpy diagram, adiabatic process is compressed to enthalpy approximately 1680 KJ/Kg of 85 DEG C of High Temperature High Pressure gaseous states, be liquefied as the enthalpy of High Temperature High Pressure liquid state at condenser isothermal: 630 KJ/Kg, its COP=(1680-630)/(1680-1480)=5.25.
Reclaim vaporization heat and heat radiation: containing in the air cycle of steam, thermosteresis is mainly come as for several aspects: 1, condenser and indirect heat exchanger between the thermosteresis of water coolant and parts; 2, the thermosteresis between air circulation duct and the external world; 3, the thermosteresis that the second interchanger cooling recirculated air causes etc.; Estimated energy organic efficiency 50-93%, first calculates by 70%.Due in compression process, electric energy becomes compression work transformation efficiency lower than 100% and heats other loss in circulation and cause COP low more more than 5.25, get temporarily 3, evaporating cold electric energy number of degrees ≈ 628/3/ (1/ (the 1-70%)) ≈ 63 that one ton of water of condensation consumes that congeals into spends so.Multiplier scale effect refers to that 3 multiply each other with (1/ (1-70%)), instead of energy recovery effect heats energy-saving effect addition with Kano.
When applicant states the low-temperature evaporation device of nitrogen circulation in the use, find because the non-condensable gases in recycle gas is air, easily cause interchanger oxygen uptake corrosion under comparatively high temps and humidity, the interchanger life-span is shorter.Therefore produced this case application, as described in Figure 6, the difference of itself and Fig. 1 is, the application is at least provided with an oxygen scavenger feedway 21 on the pipeline of the low-temperature evaporation concentration device of described nitrogen circulation.As shown in Figure 7, described oxygen scavenger feedway 21 comprises the oxygen scavenger hold-up vessel 211 connected by transport pipe 210, oxygen scavenger transferpump 212, and described transport pipe 210 is located on ducted one or more positions of pipeline between feed pipe, taper feed liquid collection unit and the first material pump, the second interchanger heat absorbing side import; In described oxygen scavenger hold-up vessel, stored oxygen scavenger is preferably 10%
sub- metabisulfite solution, or sodium sulfite solution.When operation, the oxygen concentration <0.07%(V/V in controlled circulation gas); The heat exchange wall of the stream feed liquid in operation half yearly audit interchanger, condenser and vaporizer is corrosion-free.It should be noted that, deoxygenation feedway described in the utility model also can be on the embodiment of the low-temperature evaporation concentration device described in Fig. 2-5.
Although specifically show and introduced the utility model in conjunction with preferred embodiment; but those skilled in the art should be understood that; not departing from the spirit and scope of the present utility model that appended claims limits; in the form and details the utility model is made a variety of changes, be protection domain of the present utility model.
Claims (10)
1. a low-temperature evaporation concentration device for nitrogen circulation, is characterized in that: comprise that Kano heats circulation device, an evaporation concentrator, described Kano heat circulation device comprise by pipeline circulate connect compressor, vaporizer, expansion valve, condenser; Described condenser heat absorbing side import connects feed pipe;
In described evaporation concentrator, be provided with an air circulation duct, air circulation duct comprises that a feed liquid enrichment region and a water of condensation generate district, and air circulation duct bottom is provided with one water of condensation is generated to freezing air in district and blow to the blower fan of feed liquid enrichment region;
Described feed liquid enrichment region is provided with a gas-liquid heat exchange device that carries out heat exchange for hot feed liquid and freezing air, and gas-liquid heat exchange device is connected with the heat absorbing side outlet of condenser; Below, feed liquid enrichment region is provided with a taper feed liquid collection unit;
Described water of condensation generates district and is provided with First Heat Exchanger, in feed liquid enrichment region, blow over the warm air coming and connect First Heat Exchanger heat release side entrance, the heat absorbing side outlet of First Heat Exchanger is connected with feed pipe by pipeline, water of condensation generates below, district and is provided with a taper condensation water collection portion, and taper condensation water collection portion is connected with condensation water collection tank by pipeline;
Also comprise the second interchanger, the heat absorbing side import of the second interchanger is connected refrigerant outlet and the refrigerant inlet of refrigeration agent generating apparatus with heat absorbing side outlet; The second described interchanger is located in evaporation concentrator or is located at outside evaporation concentrator;
In the time that the second described interchanger is located in evaporation concentrator: described taper feed liquid collection unit connects the heat absorbing side import of First Heat Exchanger by pipeline, the first material pump, the heat release side outlet of First Heat Exchanger connects the heat release side-entrance of the second interchanger, and the freezing air of the heat release side outlet of the second interchanger blows to blower fan;
In the time that the second described interchanger is located at outside evaporation concentrator: described taper feed liquid collection unit connects the heat release side-entrance of the second interchanger by pipeline, the first material pump, the heat release side outlet of the second interchanger connects the heat absorbing side import of First Heat Exchanger, and the freezing air of the heat release side outlet of First Heat Exchanger blows to blower fan;
On the pipeline of the low-temperature evaporation concentration device of described nitrogen circulation, be at least provided with an oxygen scavenger feedway.
2. the low-temperature evaporation concentration device of a kind of nitrogen circulation according to claim 1, it is characterized in that: described oxygen scavenger feedway comprises the oxygen scavenger hold-up vessel connected by transport pipe, oxygen scavenger transferpump, described transport pipe is connected with the pipeline of low-temperature evaporation concentration device.
3. the low-temperature evaporation concentration device of a kind of nitrogen circulation according to claim 2, is characterized in that: on the pipeline between described oxygen scavenger feedway feed pipe, taper feed liquid collection unit and the first material pump, ducted one or more positions of the second interchanger heat absorbing side import.
4. the low-temperature evaporation concentration device of a kind of nitrogen circulation according to claim 1, is characterized in that: in described oxygen scavenger hold-up vessel, stored oxygen scavenger is 10% sodium sulfite solution or 10% sodium sulfite solution.
5. according to the low-temperature evaporation concentration device of a kind of nitrogen circulation described in the arbitrary claim of claim 1-4, it is characterized in that: also comprise an indirect heat exchanger, the heat absorbing side import of described indirect heat exchanger connects feed pipe, and the heat release side-entrance of indirect heat exchanger, heat release side outlet are connected with heat absorbing side outlet, heat absorbing side import that Kano heats in the condenser of circulation device respectively; Described gas-liquid heat exchange device is connected with the outlet of the heat absorbing side of indirect heat exchanger.
6. according to the low-temperature evaporation concentration device of a kind of nitrogen circulation described in the arbitrary claim of claim 1-4: also comprise an expansion tank, recycle pump, described expansion tank water outlet is connected with recycle pump, the import of condenser heat absorbing side by pipeline, the outlet of condenser heat absorbing side is connected with indirect heat exchanger heat release side-entrance by pipeline, and indirect heat exchanger heat release side outlet connects the pipeline between expansion tank water-in or expansion tank and recycle pump.
7. according to the low-temperature evaporation concentration device of a kind of nitrogen circulation described in the arbitrary claim of claim 1-4, it is characterized in that: described gas-liquid heat exchange device is spray thrower or cooling tower without draught fan; The air circulation duct of described gas-liquid heat exchange device top is provided with a demist plate; On described feed pipe, being also provided with a shunt conduit is connected with taper feed liquid collection unit.
8. according to the low-temperature evaporation concentration device of a kind of nitrogen circulation described in the arbitrary claim of claim 1-4, it is characterized in that: in the time that the second interchanger is located in evaporation concentrator, also comprise the first equipment for separating liquid from solid, the first described material pump discharge is connected with the first outlet with the entrance of the first equipment for separating liquid from solid respectively with the import of First Heat Exchanger heat absorbing side; In the time that the second interchanger is located at outside evaporation concentrator, also comprise the first equipment for separating liquid from solid and the second equipment for separating liquid from solid, the first described material pump discharge is connected with the first outlet with the entrance of the first equipment for separating liquid from solid respectively with the second interchanger heat release side entrance, and the second described interchanger heat release side outlet is connected with the first outlet with the second equipment for separating liquid from solid entrance respectively with the import of First Heat Exchanger heat absorbing side.
9. the low-temperature evaporation concentration device of a kind of nitrogen circulation according to claim 8, it is characterized in that: described taper feed liquid collection unit is biconical feed liquid collection unit, biconical feed liquid collection unit comprises the first taper feed liquid collection unit and the second taper feed liquid collection unit, the first taper feed liquid collection unit is provided with a filtering net, and the first taper feed liquid collection unit is connected with the heat absorbing side import of First Heat Exchanger by pipeline, the first material pump; The second taper feed liquid collection unit connects the entrance of the first equipment for separating liquid from solid by the second material pump, the first outlet of the first equipment for separating liquid from solid connects the first taper feed liquid collection unit.
10. according to the low-temperature evaporation concentration device of a kind of nitrogen circulation described in the arbitrary claim of claim 1-4, it is characterized in that: described refrigeration agent generating apparatus is that Kano heats circulation device, the heat absorbing side outlet of the second interchanger connects the pipeline between compressor and vaporizer, and the heat absorbing side import of the second interchanger connects the pipeline between vaporizer and expansion valve; Or the heat absorbing side import of the second interchanger connects the pipeline between compressor and vaporizer, the heat absorbing side outlet of the second interchanger connects the pipeline between vaporizer and expansion valve.
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| CN201420150563.4U CN203754456U (en) | 2014-03-31 | 2014-03-31 | Nitrogen circulation type low-temperature evaporation concentration device |
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| CN201420150563.4U CN203754456U (en) | 2014-03-31 | 2014-03-31 | Nitrogen circulation type low-temperature evaporation concentration device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105344119A (en) * | 2015-11-30 | 2016-02-24 | 浙江奇彩环境科技有限公司 | Low-temperature spray evaporation waste water treatment device and waste water treatment method |
| CN108348821A (en) * | 2015-09-08 | 2018-07-31 | 格雷迪安特公司 | System and method for being handled water such as oil field waste by chemical coagulation |
| CN112843768A (en) * | 2021-03-04 | 2021-05-28 | 长沙永乐康仪器设备有限公司 | Method and device for recycling concentrated gas for concentrator |
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2014
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108348821A (en) * | 2015-09-08 | 2018-07-31 | 格雷迪安特公司 | System and method for being handled water such as oil field waste by chemical coagulation |
| CN105344119A (en) * | 2015-11-30 | 2016-02-24 | 浙江奇彩环境科技有限公司 | Low-temperature spray evaporation waste water treatment device and waste water treatment method |
| CN112843768A (en) * | 2021-03-04 | 2021-05-28 | 长沙永乐康仪器设备有限公司 | Method and device for recycling concentrated gas for concentrator |
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